CN110791318A - Chemical oil refining system and oil refining process - Google Patents
Chemical oil refining system and oil refining process Download PDFInfo
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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Abstract
The invention discloses a chemical oil refining system and an oil refining process. The technology introduces a new concept of synergistic reinforcement of a mesoscale micro-interface chemical reaction and a transfer process in oil refining, develops a core processing technology of on-line integration of heavy oil emulsion bed hydrogenation and distillate oil emulsion fixed bed hydrogenation, simultaneously couples and integrates a new oil refining process for producing a full chemical product aiming at the market development trend, and has the advantages of strong raw material adaptability, short process flow, low investment and production cost, high energy efficiency and resource utilization rate, cleanness, environmental protection and the like. According to the process and the method disclosed by the invention, the future chemical oil refineries do not need to build processing devices such as catalytic cracking, hydrocracking, delayed coking, heavy oil hydrogenation pretreatment and the like, and the production of full chemical products is realized, so that the process and the method are a new direction for the transformation development of the petroleum processing industry in response to new energy impact in the future.
Description
Technical Field
The invention belongs to the field of petrochemical industry, relates to a brand new technology for petroleum refining, and particularly relates to a chemical oil refining system and an oil refining process.
Background
The petroleum refining industry can produce fuels such as gasoline, kerosene, diesel oil, BTX, olefin and the like and chemical industrial raw materials, is one of the most important pillar industries of national economy, is related to the economic pulse and energy safety of the country, and has extremely important position and function in the national economy, national defense and social development.
The oil refining technology is developed to the present day, and the whole body is mature. However, with the technical progress and the improvement of the environmental protection level, the clean new energy industry is more and more valued by the industry and the society. On one hand, the rapid development of new energy vehicles may cause serious impact on the vehicle oil market in the future; on the other hand, the fuel oil tax is too heavy, which greatly weakens the profit of the finished oil. Therefore, there is a need for transformation development of refineries, and refineries producing chemicals will be the development trend in the future, and the key is to develop new processing technology with lower cost.
Disclosure of Invention
The invention aims to provide the chemical oil refining system and the oil refining process which have the advantages of strong raw material adaptability, short process flow, low investment and production cost, high energy efficiency and resource utilization rate, cleanness, environmental protection and the like.
In order to achieve the purpose, the oil refining system adopted by the invention comprises an atmospheric distillation device with a crude oil inlet, hydrogen from atmospheric residue, a catalyst and a hydrogen system at the lower end of the atmospheric distillation device is connected with an inlet of an emulsion bed hydrogenation reaction device through pipelines, a product obtained after the reaction of the emulsion bed hydrogenation reaction device enters an online separation system, a liquid-phase product obtained by the separation of the online separation system enters a vacuum distillation device for liquid-solid separation, tail oil containing solid substances extracted from the bottom of the vacuum distillation device enters a hydrogen production device, vacuum distillate oil extracted from a side line of a vacuum distillation tower, straight-run diesel oil extracted from a side line of the atmospheric distillation device, a gas-phase product obtained by the separation of the online separation system and hydrogen from the hydrogen system enter the emulsion fixed bed hydrogenation device together, and a product obtained after the reaction of the emulsion fixed bed hydrogenation device enters a gas-liquid separator, the separated gas mixture enters a gas-gas separation device to obtain dry gas, LPG and unreacted hydrogen entering a hydrogen system through a recycle hydrogen compressor, the separated liquid mixture enters a fractionating tower to obtain naphtha, light diesel oil, heavy diesel oil and wax oil, the heavy diesel oil and the wax oil return to an emulsification fixed bed hydrogenation device, the naphtha, the light diesel oil and straight-run naphtha obtained by an atmospheric distillation device enter an aromatic hydrocarbon combination device to produce aromatic hydrocarbon and byproduct residual oil, the straight-run naphtha, LPG, wax oil and byproduct residual oil obtained by the atmospheric distillation device enter a steam cracking device to produce olefin, and the byproduct cracked oil enters an aromatic hydrocarbon combination device to produce aromatic hydrocarbon.
The emulsification fixed bed hydrogenation device comprises an emulsification fixed bed hydrofining reactor and an emulsification fixed bed hydrocracking reactor which are arranged in series along the material flow direction.
The oil refining process comprises the following steps:
a. crude oil enters an atmospheric distillation device, straight-run naphtha is extracted from the top of an atmospheric distillation tower, straight-run diesel oil is extracted from the side line, and atmospheric residue oil is extracted from the bottom of the atmospheric distillation tower;
b. the normal pressure residual oil, the particle catalyst and hydrogen from a hydrogen system enter an emulsion bed hydrogenation device together, and a high-efficiency hydrogenation reaction is carried out in the emulsion bed hydrogenation device under the operating conditions of the pressure of 2-14 MPa, the temperature of 400-470 ℃ and the airspeed of 0.5-2.0 h-1The hydrogen-oil ratio is quantitative hydrogen supply, and the reaction product enters an online separation system to be separated to generate a gas-phase product and a liquid-phase product containing solid matters;
c. the liquid phase product separated on line in the step b) enters a reduced pressure distillation device for liquid-solid separation, reduced pressure distillate oil is extracted from the side line of the reduced pressure distillation tower, and tail oil containing solid matters is extracted from the bottom of the tower and is used as a gasification raw material to enter a hydrogen production device;
d. step c) extracting vacuum distillate oil from the side line of the vacuum distillation tower, feeding the vacuum distillate oil, the straight-run diesel oil extracted from the side line of the atmospheric distillation device in the step a), the gas-phase product separated on line in the step b) and hydrogen from a hydrogen system into an emulsification fixed bed hydrogenation device, and sequentially passing through an emulsification fixed bed hydrogenation refining reactor and an emulsification fixed bed hydrogenation cracking reactor which are connected in series in a mode of feeding from bottom to topThe hydrogenation reaction is carried out in the chemical reactor under the operating conditions of the pressure of 2-14 MPa, the temperature of 300-420 ℃ and the space velocity of 1.0-2.0 h-1The hydrogen-oil ratio is quantitative hydrogen supply, and the product after reaction enters a separation system for gas-liquid separation;
e. after a reaction product of the emulsification fixed bed hydrogenation device enters a separation system, gas-liquid separation is carried out by a gas-liquid separation device, a separated gas mixture enters the gas-gas separation device to obtain unreacted hydrogen, dry gas and LPG, and the unreacted hydrogen enters a hydrogen system through a recycle hydrogen compressor; the separated liquid mixture enters a fractionating tower to obtain naphtha, light diesel oil, heavy diesel oil and wax oil;
f. returning the heavy diesel oil and the wax oil obtained in the step e) to an emulsification fixed bed hydrogenation device, and entering an emulsification fixed bed hydrocracking reactor to convert the heavy diesel oil and the wax oil into naphtha and light diesel oil;
g. feeding the straight-run naphtha obtained in the step a) and the naphtha and light diesel oil obtained in the step e) into an aromatics complex device to produce aromatics and obtain a byproduct raffinate oil;
h. feeding the straight-run naphtha obtained in the step a), the LPG obtained in the step e), the wax oil and the raffinate oil obtained in the step g) into a steam cracking device to produce olefin and obtain a byproduct of cracked oil;
i. and h), introducing the pyrolysis oil obtained in the step h) into an aromatic hydrocarbon integrated unit to produce aromatic hydrocarbon.
The catalyst adopted by the hydrogenation device of the emulsion bed in the step b) is an iron-based or molybdenum-based catalyst, and the particle size distribution range of the catalyst is 10-300 mu m.
The sizes of hydrogen microbubbles serving as dispersed phases in the emulsion bed hydrogenation device and the emulsion fixed bed hydrogenation device are 10-1000 mu m, and the gas-liquid phase interface area is 2000-20000 m2/m3。
The emulsion bed hydrogenation device can be used for processing heavy oil with high metal content, high asphaltene content, high solid content, high carbon residue content and high sulfur nitrogen content, wherein the sulfur content in the heavy oil is 0.1-8 wt%, the nitrogen content is 0.1-1.0 wt%, the solid content is 0.01-1 wt%, the metal (Fe + Ni + V) content is 10-2000 ppm, the asphaltene content is 0.1-25 wt%, and the carbon residue content is 1-40 wt%.
The total heavy oil conversion rate of the emulsion bed hydrogenation device is 85-99%, the asphaltene conversion rate is 75-95%, and the hydrogen consumption is 1-3 wt%; the total liquid yield is 85-95 wt%, the tail oil yield is 2-6 wt%, in the total liquid yield, the naphtha fraction accounts for 5-15 wt%, the diesel fraction accounts for 30-40 wt%, and the wax oil fraction accounts for 30-40 wt%; the desulfurization rate is 50-85 wt%, the denitrification rate is 30-50 wt%, and the demetallization rate is more than 90 wt%.
The total liquid yield of the emulsifying fixed bed hydrogenation device is 93-98%, and the desulfurization rate is 90-99%.
The emulsifying fixed bed hydrogenation device is formed by grading a catalyst with one or more mixed active components of molybdenum, nickel, tungsten and cobalt, and the catalyst is filled in layers in the shape of one or more of clover, clover and dentate sphere.
The aromatic hydrocarbon potential of naphtha obtained by the fractionating tower is more than 40%, and the BMCI value of wax oil is 6-18.
The invention develops a core processing technology of on-line integration of heavy oil emulsion bed hydrogenation and distillate oil emulsion fixed bed hydrogenation by introducing a new concept of synergistic reinforcement of a mesoscale micro-interface chemical reaction and a transfer process, simultaneously couples and integrates a new oil refining process for producing a full chemical product aiming at the market development trend, and has the advantages of strong raw material adaptability, short process flow, low investment and production cost, high energy efficiency and resource utilization rate, cleanness, environmental protection and the like. According to the process disclosed by the invention, the chemical oil refinery does not need to build processing devices such as catalytic cracking, hydrocracking, delayed coking, heavy oil hydrogenation pretreatment and the like, and simultaneously realizes the production of full chemical products, so that the process is a new direction for the transformation development of the petroleum processing industry in response to the new energy impact in the future.
Drawings
FIG. 1 is a production process diagram of the present invention.
Detailed Description
The invention is described in further detail below with reference to fig. 1:
referring to fig. 1, the system of the present invention includes an atmospheric distillation unit with a crude oil inlet, hydrogen from atmospheric residue, catalyst and hydrogen system at the lower end of the atmospheric distillation unit is connected with the inlet of an emulsion bed hydrogenation reaction unit through a pipeline, the product after the reaction of the emulsion bed hydrogenation reaction unit enters an on-line separation system, the liquid phase product separated by the on-line separation system enters a vacuum distillation unit for liquid-solid separation, the tail oil containing solid matter extracted from the bottom of the vacuum distillation unit enters a hydrogen production unit, the vacuum distillate oil extracted from the side line of the vacuum distillation tower and the straight-run diesel oil extracted from the side line of the atmospheric distillation unit, the gas phase product separated by the on-line separation system and the hydrogen from the hydrogen system enter the emulsion fixed bed hydrogenation unit together, the emulsion fixed bed hydrogenation unit includes an emulsion fixed bed hydrofining reactor and an emulsion fixed bed hydrocracking reactor connected, the product after the reaction of the emulsification fixed bed hydrogenation device enters a gas-liquid separator of a separation system for gas-liquid separation, the separated gas mixture enters a gas-gas separation device to obtain dry gas, LPG and unreacted hydrogen entering a hydrogen system through a recycle hydrogen compressor, the separated liquid mixture enters a fractionating tower to obtain naphtha, light diesel oil, heavy diesel oil and wax oil, the heavy diesel oil and the wax oil return to the emulsification fixed bed hydrogenation device, the naphtha, the light diesel oil and straight-run naphtha obtained by an atmospheric distillation device enter an aromatic hydrocarbon combination device to produce aromatic hydrocarbon and byproduct residual oil, the straight-run naphtha, LPG, wax oil and byproduct residual oil obtained by the atmospheric distillation device enter a steam cracking device to produce olefin, and the byproduct cracked oil enters an aromatic hydrocarbon combination device to produce aromatic hydrocarbon.
Referring to fig. 1, the process of the present invention comprises the following steps:
a. crude oil enters an atmospheric distillation device, straight-run naphtha is extracted from the top of an atmospheric distillation tower, straight-run diesel oil is extracted from the side line, and atmospheric residue oil is extracted from the bottom of the atmospheric distillation tower;
b. the method comprises the steps of enabling atmospheric residue, a particle catalyst and hydrogen from a hydrogen system to enter an emulsion bed hydrogenation reactor, and carrying out efficient hydrogenation reaction in an emulsion bed hydrogenation device under the operating conditions of pressure of 2-14 MPa, temperature of 400-470 ℃ and airspeed of 0.5-2.0 h-1The hydrogen-oil ratio is quantitative hydrogen supply, and the product after reaction enters an online separation system and is separated into a gas-phase product and a liquid-phase product containing solid matters;
c. the liquid phase product separated on line in the step b) enters a reduced pressure distillation device for liquid-solid separation, reduced pressure distillate oil is extracted from the side line of the reduced pressure distillation tower, and tail oil containing solid matters is extracted from the bottom of the tower and is used as a gasification raw material to enter a hydrogen production device;
d. step c) vacuum distillate oil extracted from the side line of the vacuum distillation tower, straight-run diesel oil extracted from the side line of the atmospheric distillation device in the step a), gas-phase products separated on line in the step b) and hydrogen from a hydrogen system enter an emulsification fixed bed hydrogenation device, and hydrogenation reaction is carried out through an emulsification fixed bed hydrofining reactor and an emulsification fixed bed hydrocracking reactor which are connected in series in a mode of feeding in and feeding out from the bottom, wherein the operation conditions are that the pressure is 2-14 MPa, the temperature is 300-420 ℃, and the space velocity is 1.0-2.0 h-1The hydrogen-oil ratio is quantitative hydrogen supply, and the product after reaction enters a separation system for gas-liquid separation;
e. after a reaction product of the emulsification fixed bed hydrogenation device enters a separation system, gas-liquid separation is carried out by a gas-liquid separation device, a separated gas mixture enters the gas-gas separation device to obtain unreacted hydrogen, dry gas and LPG, and the unreacted hydrogen enters a hydrogen system through a recycle hydrogen compressor; the separated liquid mixture enters a fractionating tower to obtain naphtha, light diesel oil, heavy diesel oil and wax oil;
f. returning the heavy diesel oil and the wax oil obtained in the step e) to an emulsification fixed bed hydrogenation device, and entering an emulsification fixed bed hydrocracking reactor to convert the heavy diesel oil and the wax oil into naphtha and light diesel oil;
g. feeding the straight-run naphtha obtained in the step a) and the naphtha and light diesel oil obtained in the step e) into an aromatics complex device to produce aromatics and obtain a byproduct raffinate oil;
h. feeding the straight-run naphtha obtained in the step a), the LPG obtained in the step e), the wax oil and the raffinate oil obtained in the step g) into a steam cracking device to produce olefin and obtain a byproduct of cracked oil;
i. and h), introducing the pyrolysis oil obtained in the step h) into an aromatic hydrocarbon integrated unit to produce aromatic hydrocarbon.
The catalyst adopted by the hydrogenation device of the emulsion bed in the step b) is an iron-based or molybdenum-based catalyst, and the particle size distribution range of the catalyst is 10-300 mu m. The sizes of the hydrogen microbubbles of the dispersed phase in the hydrogenation device of the emulsification bed and the hydrogenation device of the emulsification fixed bed are between10 to 1000 μm, and a gas-liquid interface area of 2000 to 20000m2/m3. The diffusion resistance of a liquid film in the constructed mesoscopic reaction system is greatly reduced, the phase interface is greatly improved, the hydrogen dissolving and transferring capability is enhanced, and the hydrogenation reaction efficiency is obviously improved.
The total conversion rate of heavy oil of the emulsion bed hydrogenation device is 85-99%, the conversion rate of asphaltene is 75-95%, the hydrogen consumption is 1-3 wt%, the total liquid yield of the emulsion bed hydrogenation device is 85-95 wt%, the yield of tail oil is 2-6 wt%, in the total liquid yield, the naphtha fraction accounts for 5-15 wt%, the diesel fraction accounts for 30-40 wt%, the wax oil fraction accounts for 30-40 wt%, the desulfurization rate of the emulsion bed hydrogenation device is 50-85 wt%, the denitrification rate is 30-50 wt%, and the demetallization rate is more than 90 wt%.
The emulsifying bed hydrogenation device has strong adaptability to raw materials, can process heavy oil with high metal content, high asphaltene content, high solid content, high carbon residue and high sulfur and nitrogen content, wherein the sulfur content in the raw materials is 0.1-8 wt%, the nitrogen content is 0.1-1.0 wt%, the solid content is 0.01-1 wt%, the metal (Fe + Ni + V) content is 10-2000 ppm, the asphaltene content is 0.1-25 wt%, the carbon residue content is 1-40 wt%, and the single set processing capacity of the emulsifying bed hydrogenation device is 200-500 ten thousand tons per year.
The total liquid yield of the hydrogenation device of the emulsifying fixed bed is 93-98%, the desulfurization rate is 90-99%, the hydrogenation device of the emulsifying fixed bed is formed by grading a catalyst with one or more mixed active components of molybdenum, nickel, tungsten and cobalt, and the catalyst is in the shape of one or more of clover, clover and dentate sphere and is filled in layers.
The aromatic hydrocarbon potential of naphtha obtained by the fractionating tower is more than 40%, and the BMCI value of wax oil is 6-18.
The wax oil obtained in the step e) can be returned to an emulsification fixed bed hydrogenation device for further conversion to produce naphtha and light diesel oil, or can enter a steam cracking device for olefin production, and is adjusted according to market demands, wherein the adjustment ratio is 0-1, the straight-run naphtha obtained in the same step a) can enter the steam cracking device for olefin production, or can enter an aromatic hydrocarbon combination device for aromatic hydrocarbon production, and is adjusted according to market demands, and the adjustment ratio is 1-0.
The invention adopts the hydrogenation technology of the emulsion bed to efficiently and cleanly convert heavy fraction oil in crude oil into distillate oil in one step, can replace four processing technologies of heavy oil prehydrogenation (RDS), hydrocracking, catalytic cracking and delayed coking in the oil refining process, and greatly shortens the process flow of the traditional oil refining process. The process only produces chemical products such as olefin, aromatic hydrocarbon and the like, and does not produce liquid fuel oil so as to deal with the impact of new energy on the traditional oil refining industry.
The hydrogenation device of the emulsifying bed, the online separation system and the hydrogenation device of the emulsifying fixed bed are in the same system and are an online integrated process.
The hydrogen production device can be coupled with a fuel gas-steam combined cycle power generation system and a C1 chemical plant.
The invention has the following beneficial effects:
1. the invention introduces a new concept of synergy and reinforcement of the micro-interface chemical reaction and the transfer process of mesoscale in oil refining technology, greatly reduces the diffusion resistance of a liquid film in a constructed mesoscopic reaction system, greatly increases the phase interface, strengthens the hydrogen dissolving and transferring capability, and obviously improves the hydrogenation reaction efficiency.
2. The emulsion bed hydrogenation technology can replace four technologies of heavy oil pre-hydrogenation (RDS), hydrocracking, catalytic cracking and delayed coking, realize one-step efficient clean conversion of heavy distillate oil in crude oil, and greatly shorten the process flow of petroleum processing; but also can process heavy oil with high metal content, high asphaltene content, high carbon residue content and high solid content, and better solves the problems of heavy oil and light oil of the world.
3. Compared with the existing fixed bed hydrogenation technology, the emulsification fixed bed hydrogenation technology of the invention not only can improve the processing capacity, but also can increase the hydrogenation reaction effect and reduce the operation severity and energy consumption.
4. According to the invention, the future chemical oil refinery comprises main processing devices such as an atmospheric distillation device, a vacuum distillation device, an emulsion bed hydrogenation device, a fixed bed emulsion hydrogenation device, an aromatic hydrocarbon combination device, a steam cracking device, a hydrogen production device and the like, compared with the existing petroleum processing technical route for producing chemicals, on one hand, a catalytic cracking device, a hydrocracking device, a heavy oil hydrogenation pretreatment device and a coking device are not needed, and the number of the main processing devices is reduced by 2-3 sets; on the other hand, only chemical products such as olefin, aromatic hydrocarbon and the like are produced, liquid fuel oil is not produced, the problem of excessive oil products can be well solved, the method is a new direction for transformation development of the petroleum processing industry in the future, and has good market competitiveness.
Claims (10)
1. A chemical oil refining system, comprising: the method comprises the steps that an atmospheric distillation device with a crude oil inlet is included, hydrogen from an atmospheric residue, a catalyst and a hydrogen system at the lower end of the atmospheric distillation device is connected with an inlet of an emulsion bed hydrogenation reaction device through a pipeline, a product obtained after the reaction of the emulsion bed hydrogenation reaction device enters an online separation system, a liquid-phase product separated by the online separation system enters a vacuum distillation device for liquid-solid separation, tail oil containing solid substances and extracted from the bottom of the vacuum distillation device enters a hydrogen production device, vacuum distillate oil extracted from a side line of a vacuum distillation tower, straight-run diesel oil extracted from a side line of the atmospheric distillation device, a gas-phase product separated by the online separation system and hydrogen from a hydrogen system enter an emulsion fixed bed hydrogenation device, the product obtained after the reaction of the emulsion fixed bed hydrogenation device enters a gas-liquid separator of the separation system for gas-liquid separation, and a separated gas mixture enters, LPG and unreacted hydrogen entering a hydrogen system through a recycle hydrogen compressor, feeding a separated liquid mixture into a fractionating tower to obtain naphtha, light diesel oil, heavy diesel oil and wax oil, returning the heavy diesel oil and the wax oil to an emulsification fixed bed hydrogenation device, feeding the naphtha, the light diesel oil and straight-run naphtha obtained by an atmospheric distillation device into an aromatics complex device to produce aromatic hydrocarbon and byproduct residual oil, feeding the straight-run naphtha, the LPG, the wax oil and the byproduct residual oil obtained by the atmospheric distillation device into a steam cracking device to produce olefin, and feeding the byproduct cracked oil into the aromatics complex device to produce aromatic hydrocarbon.
2. The chemical refinery system of claim 1, wherein: the emulsification fixed bed hydrogenation device comprises an emulsification fixed bed hydrofining reactor and an emulsification fixed bed hydrocracking reactor which are arranged in series along the material flow direction.
3. A chemical refinery process comprising the steps of:
a. crude oil enters an atmospheric distillation device, straight-run naphtha is extracted from the top of an atmospheric distillation tower, straight-run diesel oil is extracted from the side line, and atmospheric residue oil is extracted from the bottom of the atmospheric distillation tower;
b. the normal pressure residual oil, the particle catalyst and hydrogen from a hydrogen system enter an emulsion bed hydrogenation device together, and a high-efficiency hydrogenation reaction is carried out in the emulsion bed hydrogenation device under the operating conditions of the pressure of 2-14 MPa, the temperature of 400-470 ℃ and the airspeed of 0.5-2.0 h-1The hydrogen-oil ratio is quantitative hydrogen supply, and the reaction product enters an online separation system to be separated to generate a gas-phase product and a solid-liquid-phase-containing product;
c. the liquid phase product obtained by the on-line separation in the step b) enters a reduced pressure distillation device for liquid-solid separation, reduced pressure distillate oil is extracted from the side line of the reduced pressure distillation tower, and solid-containing tail oil extracted from the bottom of the tower is taken as gasification raw material to be sent to a hydrogen production device;
d. vacuum distillate oil extracted from the side line of the vacuum distillation tower in the step c), straight-run diesel oil extracted from the side line of the atmospheric distillation device in the step a), gas-phase products separated on line in the step b) and hydrogen from a hydrogen system enter an emulsification fixed bed hydrogenation device, and hydrogenation reaction is carried out by sequentially passing through an emulsification fixed bed hydrofining reactor and an emulsification fixed bed hydrocracking reactor which are connected in series in a mode of feeding in and feeding out from bottom to top, wherein the operation conditions are that the pressure is 2-14 MPa, the temperature is 300-420 ℃, and the space velocity is 1.0-2.0 h-1The hydrogen-oil ratio is quantitative hydrogen supply, and the reaction product enters a separation system to carry out gas-liquid separation;
e. after the reaction product of the emulsification fixed bed hydrogenation device in the step d) enters a separation system, a gas-liquid separation device is used for separating gas-phase and liquid-phase products, the separated gas mixture enters the gas-gas separation device for gas-phase product separation to obtain unreacted hydrogen, dry gas and LPG, the unreacted hydrogen enters a hydrogen system through a recycle hydrogen compressor, and the separated liquid mixture enters a fractionating tower to produce naphtha, light diesel oil, heavy diesel oil and wax oil;
f. returning the heavy diesel oil and the wax oil obtained in the step e) to an emulsification fixed bed hydrogenation device, and allowing the heavy diesel oil and the wax oil to enter an emulsification fixed bed hydrocracking reactor for further conversion into naphtha and light diesel oil;
g. feeding the straight-run naphtha obtained in the step a) and the naphtha and light diesel oil obtained in the step e) into an aromatics complex device to produce aromatics and obtain a byproduct raffinate oil;
h. feeding the straight-run naphtha obtained in the step a), the LPG obtained in the step e), the wax oil and the raffinate oil obtained in the step g) into a steam cracking device to produce olefin and obtain a byproduct of cracked oil;
i. and h), introducing the pyrolysis oil obtained in the step h) into an aromatic hydrocarbon integrated unit to produce aromatic hydrocarbon.
4. The chemical refinery process of claim 1, wherein: the catalyst adopted by the hydrogenation device of the emulsion bed in the step b) is an iron-based or molybdenum-based catalyst, and the particle size distribution range of the catalyst is 10-300 mu m.
5. The chemical refinery process of claim 1, wherein: the sizes of hydrogen microbubbles serving as dispersed phases in the hydrogenation device of the emulsion bed and the hydrogenation device of the emulsion fixed bed are 10-1000 mu m, and the gas-liquid ratio phase interface area is 2000-20000 m2/m3。
6. The chemical refinery process of claim 1, wherein: the emulsifying bed hydrogenation device can process heavy oil with high metal content, high asphaltene content, high solid content, high carbon residue content and high sulfur nitrogen content, wherein the sulfur content in the heavy oil is 0.1-8 wt%, the nitrogen content is 0.1-1.0 wt%, the solid content is 0.01-1 wt%, the metal (Fe + Ni + V) content is 10-2000 ppm, the asphaltene content is 0.1-25 wt%, and the carbon residue content is 1-40 wt%.
7. The chemical refinery process of claim 1, wherein: the total conversion rate of heavy oil of the emulsion bed hydrogenation device is 85-99%, the conversion rate of asphaltene is 75-95%, the hydrogen consumption is 1-3 wt%, the total liquid yield is 85-95 wt%, the tail oil yield is 2-6 wt%, the proportion of naphtha fraction in the liquid product is 5-15 wt%, the proportion of diesel fraction is 30-40 wt%, the proportion of wax oil fraction is 30-40 wt%, the desulfurization rate is 50-85 wt%, the denitrification rate is 30-50 wt%, and the demetallization rate is more than 90 wt%.
8. The chemical refinery process of claim 1, wherein: the total liquid yield of the hydrogenation device of the emulsification fixed bed is 93-98%, and the desulfurization rate is 90-99%.
9. The chemical refinery process of claim 1, wherein: the emulsifying fixed bed hydrogenation device is formed by grading a catalyst with one or more mixed active components of molybdenum, nickel, tungsten and cobalt, and the catalyst is filled in layers in the shape of one or more of clover, clover and dentate sphere.
10. The chemical refinery process of claim 1, wherein: the aromatic hydrocarbon potential of naphtha obtained by the fractionating tower is more than 40%, and the BMCI value of wax oil is 6-18.
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