An integrated hydrogenation process and hydrogenation system for crude oil-to-chemicals

Abstract

The present invention discloses an integrated hydrogenation process and system for producing crude oil-based chemicals. The system comprises a first fractionation unit, a first ebullated-bed reaction zone, a first gas-liquid separator, a second ebullated-bed reaction zone, a second gas-liquid separator, a first fixed-bed reaction zone, a second fixed-bed reaction zone, a second fractionation unit, a third gas-liquid separation unit, a fourth gas-liquid separator, and a fourth fractionation unit. Also provided is an integrated hydrogenation process for producing crude oil-based chemicals, coupling the separation unit, ebullated-bed heavy oil hydrogenation, and fixed-bed hydrogenation to achieve efficient conversion of crude oil into light naphtha and heavy naphtha, chemical raw materials. The process of the present invention efficiently and organically couples the reaction units, achieving a crude oil-to-chemical conversion rate exceeding 85%. Furthermore, through optimized device coupling, device investment and energy consumption can be significantly reduced.

Description

Technical Field

[0001] The present invention belongs to the technical field of petrochemical industry, and in particular relates to an integrated hydrogenation process for producing chemicals from crude oil. Background Art

[0002] Amidst the dilemma of diminishing returns in refined oil production, crude oil to chemicals (COTC) technology may become the next evolutionary trend in the oil refining sector. In recent years, some companies have begun elevating refining and chemical integration to a new level of crude oil to chemicals through integrated innovations in traditional refining processes or by directly overturning traditional refining processes. Based on the current state of technology and future development trends, COTC technology can be categorized into two categories: maximizing crude oil to chemicals and directly converting crude oil to chemicals. The yield of crude oil to basic petrochemical feedstocks for each process route generally ranges from 5% to 10% for traditional fuel-based refineries, 10% to 20% for conventional integrated refining and chemical plants, and over 40% and potentially even up to 80% for crude oil to chemicals plants.

[0003] ExxonMobil's direct crude oil steam cracking technology to produce olefins is a prime example of crude oil-to-chemicals technology. Its most significant feature is the omission of refining units such as atmospheric and vacuum distillation, and the inclusion of a flash tank between the convection and radiant sections of the cracking furnace, significantly simplifying the process. However, this technology is primarily designed for light crude oils, such as condensate, and presents challenges with conventional or heavy crude oils.

[0004] Maximizing crude oil production into chemicals is based on typical refining techniques, optimizing traditional refining processes to maximize the production of chemical feedstocks for use in integrated petrochemical plants. This approach involves adding additional process units, such as hydrocracking, to convert heavy products such as wax oil and residual oil from the crude oil refining process into lighter products while simultaneously increasing the hydrogen-to-carbon ratio. Leveraging existing, mature technologies and reconfiguring them, the yield of basic petrochemical feedstocks can be significantly increased to 40% to 50%. This type of technology primarily uses atmospheric and vacuum distillation units to cut crude oil, processing the individual fractions through existing equipment to produce chemical feedstocks. Currently, this type of technology operates independently using individual units, resulting in poor device coupling. Summary of the Invention

[0005] To address the shortcomings of existing technologies, the present invention provides an integrated crude oil-to-chemicals hydrogenation process and system. This system couples a separation unit, an ebullating-bed heavy oil hydrogenation unit, and a fixed-bed hydrogenation unit to efficiently convert crude oil into light and heavy naphtha chemical feedstocks. The light naphtha provides feedstock for steam cracking to produce olefins, while the heavy naphtha provides feedstock for catalytic reforming to produce aromatics. The process flow of the present invention efficiently and organically couples the reaction units, resulting in low energy consumption and investment.

[0006] A first aspect of the present invention provides an integrated hydrogenation process for producing chemicals from crude oil, the hydrogenation process comprising the following steps:

[0007] (1) Under separation conditions, the crude oil is separated to obtain a first light fraction, a first middle fraction, and a first heavy fraction;

[0008] (2) The first heavy fraction obtained in step (1) enters the first ebullated bed reaction zone, contacts with hydrogen and reacts, and the reaction products are separated to obtain a first gas phase stream and a first liquid phase stream;

[0009] (3) the first liquid stream obtained in step (2) enters a second ebullated bed reaction zone, contacts with hydrogen and reacts, and the reaction product is separated to obtain a second gas stream and a second liquid stream, and the second liquid stream is separated to obtain a second light fraction, a second middle fraction, and a second heavy fraction;

[0010] (4) The first gas-phase stream obtained in step (2) and the second gas-phase stream obtained in step (3) enter the first fixed-bed reaction zone, contact with hydrogen to react, and the reaction products are separated to obtain a third gas-phase stream and a third liquid-phase stream;

[0011] (5) the first middle distillate obtained in step (1), the second light distillate obtained in step (3), the second middle distillate obtained in step (3), and the third gaseous stream obtained in step (4) enter a second fixed-bed reaction zone, contact with hydrogen to react, and the reaction products are separated to obtain a fourth gaseous stream and a fourth liquid stream;

[0012] (6) The third liquid phase stream obtained in step (4) and the fourth liquid phase stream obtained in step (5) are mixed and separated to obtain light hydrocarbons, light naphtha, heavy naphtha and hydrogenated heavy oil.

[0013] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the crude oil in step (1) can be crude oil of different species and sources, such as at least one of low-sulfur paraffin-based crude oil, low-sulfur intermediate-based crude oil, sulfur-containing intermediate-based crude oil, and sulfur-containing cycloalkyl crude oil.

[0014] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the separation in step (1) can adopt any one of flash distillation, atmospheric distillation, and atmospheric and vacuum distillation processes. Those skilled in the art can select an appropriate separation method according to the properties of the processed raw oil.

[0015] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific embodiment, the cutting temperature of the first light fraction and the first middle fraction in step (1) is 60-230°C, preferably 65-200°C; the cutting temperature of the first middle fraction and the first heavy fraction is 145-400°C, preferably 175-380°C. The first light fraction is generally controlled to be a naphtha fraction, the first middle fraction is generally controlled to be a diesel fraction or a mixed fraction of diesel and wax oil, and the first heavy fraction is generally controlled to be a residue, specifically atmospheric residue and / or vacuum residue.

[0016] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific embodiment, the reaction conditions of the first ebullated bed reaction zone are as follows: reaction temperature of 350-450°C, preferably 380-430°C, reaction pressure of 10.0-19.0 MPa, preferably 13.0-18.0 MPa, hydrogen-to-oil volume ratio of 300-1000, preferably 400-600, liquid hourly volume space velocity of 0.1-3.0 h -1 , preferably 0.15~1.0h -1 .

[0017] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific embodiment, the reaction conditions of the second ebullated bed reaction zone are as follows: reaction temperature of 350-450°C, preferably 380-430°C, reaction pressure of 10.0-19.0 MPa, preferably 13.0-18.0 MPa, hydrogen-to-oil volume ratio of 300-1000, preferably 400-600, liquid hourly volume space velocity of 0.1-3.0 h -1 , preferably 0.15~1.0h -1 .

[0018] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, a single ebullated bed reactor is set in the first ebullated bed reaction zone in step (2) and the second ebullated bed reaction zone in step (3), or more than two ebullated bed reactors can be set. Preferably, the two or more ebullated bed reactors are configured in series, and a gas-liquid separator is further provided between the reactors; the ebullated bed reactor can be a reactor with an external circulation cup, or it can be a STRONG ebullated bed reactor with a three-phase separator developed by Sinopec (Dalian) Petrochemical Research Institute Co., Ltd.

[0019] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific embodiment, the ebullated-bed reactors in the first and second ebullated-bed reaction zones are loaded with an ebullated-bed hydrogenation catalyst. The catalyst comprises a support and an active metal, wherein the active metal may be one or more of nickel, cobalt, molybdenum, and tungsten; and the support may be one or more of alumina, alumina-silica, silica, and titanium oxide. The ebullated-bed hydrogenation catalyst may be a commercially available product or prepared according to existing publicly available methods, such as the FEM-10 or FES-31 ebullated-bed hydrogenation catalyst developed by Sinopec (Dalian) Petrochemical Research Institute Co., Ltd.

[0020] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the cutting temperature of the second light fraction and the second middle fraction is 300-400°C, preferably 350-380°C; the cutting temperature of the second middle fraction and the second heavy fraction is 480-550°C, preferably 500-540°C.

[0021] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the second liquid phase stream is separated to obtain a second light fraction A, a second light fraction B, a second middle fraction and a second heavy fraction; wherein, the second light fraction B can be recycled in whole or in part to the first ebullated bed reaction zone for treatment, and when a part of it is recycled to the first ebullated bed reaction zone for treatment, the remaining part enters the second fixed bed reaction zone for treatment; the cutting temperature of the second light fraction A and the second light fraction B is 210-330°C, preferably 240-330°C; the cutting temperature of the second light fraction B and the second middle fraction is 300-400°C, preferably 350-380°C.

[0022] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific embodiment, the reaction conditions in the first fixed bed reaction zone are as follows: reaction temperature of 280-350°C, preferably 300-330°C; reaction pressure of 10-19 MPa, preferably 13-18 MPa; hydrogen-to-oil volume ratio of 500-1200, preferably 700-1000; liquid hourly volume space velocity of 0.5-3.0 h -1 , preferably 1.0 to 2.0 hours -1 .

[0023] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, more than one fixed bed reactor is provided in the first fixed bed reaction zone, and a one-pass process can be adopted. The catalyst used in the reactor of the first fixed bed reaction zone can be an existing naphtha hydrorefining catalyst, and the catalyst includes a carrier and an active metal, wherein the active metal can be one or more of nickel, cobalt, molybdenum or tungsten; the carrier can be one or more of alumina, silica, alumina-silica, and titanium oxide.

[0024] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific embodiment, the reaction conditions of the second fixed bed reaction zone are as follows: reaction temperature is 350-400°C, preferably 360-390°C; hydrogen-to-oil volume ratio is 700-1500, preferably 800-1200; liquid hourly volume space velocity is 0.5-3.0h -1 , preferably 1.0 to 2.0 hours -1 ; The reaction pressure is 12.0~16.0MPa, preferably 13.0~15.0MPa.

[0025] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the first light fraction obtained in step (1) can be fed into the first fixed-bed reaction zone for treatment, or directly mixed with the light naphtha obtained in step (6) without hydrogenation treatment and used as a feedstock for producing ethylene in a steam cracking unit.

[0026] Furthermore, in the above-mentioned integrated hydrogenation process for producing crude oil-to-chemicals, as a specific embodiment, the second heavy fraction in step (3) can be recycled to the first ebullated-bed reaction zone and / or the second ebullated-bed reaction zone for treatment, or can be discharged as a feedstock for coking, solvent deasphalting, partial oxidation hydrogen production (POX), and other units. Specifically, it can be used as a coking feedstock to produce low-sulfur petroleum coke, or as a feedstock for POX hydrogen production, or it can be fed into a solvent deasphalting unit to generate deasphalted oil and deoiled asphalt, the deasphalted oil being fed into a hydrocracking unit for treatment, and the deoiled asphalt being used as a feedstock for POX hydrogen production.

[0027] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific embodiment, the light naphtha in step (6) can be used as a raw material for producing ethylene in a steam cracking unit, and the heavy naphtha can be used as an aromatics raw material.

[0028] Furthermore, in the above-mentioned integrated hydrogenation process for crude oil to chemicals, as a specific embodiment, the second fixed-bed reaction zone can be equipped with a single fixed-bed reactor, or two or more fixed-bed reactors can be equipped with the fixed-bed reactor. Preferably, the two or more fixed-bed reactors are arranged in series, and more preferably, two fixed-bed reactors are arranged in series. When two fixed-bed reactors are used, the first reactor and the second reactor are configured as a refining reactor and a cracking reactor, respectively. The second fixed-bed reaction zone can adopt any of a single-stage series one-pass flow, a single-stage series partial circulation flow, or a single-stage series full circulation flow, preferably a single-stage series full circulation flow.

[0029] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, when two or more fixed-bed reactors are arranged in the second fixed-bed reaction zone, a stripping tower can be set up to remove H2S, NH3, etc. according to the impurity content in the processed raw materials. The gas phase obtained by the stripping tower enters the subsequent cold high-fraction and circulating hydrogen purification and recovery units for treatment.

[0030] Furthermore, in the above-mentioned integrated crude oil-to-chemicals hydrogenation process, as a specific embodiment, the fixed-bed reactor in the second fixed-bed reaction zone is loaded with a fixed-bed hydrogenation catalyst, specifically a hydrorefining catalyst and / or a hydrocracking catalyst. The catalyst can be a commercially available product or can be prepared in-house using methods disclosed in the prior art.

[0031] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the fourth gaseous phase stream in step (5) is used as circulating hydrogen after purification treatment. The purification treatment generally includes hydrogen purification treatment such as desulfurization treatment and membrane separation. The hydrogen concentration in the hydrogen-rich gas after membrane separation is generally required to reach more than 95%. After being pressurized by a circulating hydrogen compressor, it is circulated to each reaction unit for use as circulating hydrogen.

[0032] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the reaction products in step (2) are separated to obtain a first gas phase stream and a first liquid phase stream, and during the separation, recycled hydrogen and / or new hydrogen are introduced as a stripping medium to be separated together with the reaction products.

[0033] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the reaction products in step (3) are separated to obtain a second gas phase stream and a second liquid phase stream, and during the separation, recycled hydrogen and / or new hydrogen are introduced as a stripping medium to separate together with the reaction products.

[0034] Furthermore, in the above-mentioned integrated hydrogenation process for producing chemicals from crude oil, as a specific implementation scheme, the hydrogenated heavy oil in step (6) is recycled back to the second fixed-bed reaction zone for treatment.

[0035] A second aspect of the present invention provides an integrated hydrogenation system for producing crude oil-based chemicals, the system comprising a first fractionation unit, a first ebullated bed reaction zone, a first gas-liquid separator, a second ebullated bed reaction zone, a second gas-liquid separator, a first fixed bed reaction zone, a second fixed bed reaction zone, a second fractionation unit, a third gas-liquid separation unit, a fourth gas-liquid separator, and a fourth fractionation unit;

[0036] a first fractionation unit, which is used to receive and separate crude oil, and obtain a first light fraction, a first middle fraction and a first heavy fraction after the crude oil is separated;

[0037] a first ebullated bed reaction zone, which is used to receive the first heavy fraction from the first fractionation unit and contact it with hydrogen to react;

[0038] a first gas-liquid separator, which is used to receive and separate the reaction product from the first ebullated bed reaction zone to obtain a first gas phase material flow and a first liquid phase material flow after separation;

[0039] a second ebullated bed reaction zone, which is used to receive the first liquid phase stream from the first gas-liquid separator and contact it with hydrogen to react;

[0040] a second gas-liquid separator, which is used to receive the reaction product from the second ebullated bed reaction zone and obtain a second gas phase material flow and a second liquid phase material flow after separation;

[0041] a second fractionation unit, which is used to receive the second liquid phase stream from the second gas-liquid separator and obtain a second light fraction, a second middle fraction and a second heavy fraction after separation;

[0042] a first fixed bed reaction zone, which is used to receive the first gas-phase material flow from the first gas-liquid separator and the second gas-phase material flow from the second gas-liquid separator, and contact them with hydrogen to react;

[0043] a third gas-liquid separator, which is used to receive the reaction product from the first fixed bed reaction zone and obtain a third gas phase material flow and a third liquid phase material flow after separation;

[0044] a second fixed-bed reaction zone, which is used to receive the first middle distillate from the first fractionation unit, the second light fraction and the second middle distillate from the second fractionation unit, and the third gaseous stream from the third separator, and contact them with hydrogen for reaction;

[0045] a fourth gas-liquid separator, which is used to receive the reaction product from the second fixed-bed reaction zone and obtain a fourth gas phase material flow and a fourth liquid phase material flow after separation;

[0046] The third fractionation unit is used to receive the third liquid phase stream from the third gas-liquid separation unit and the fourth liquid phase stream from the fourth gas-liquid separator, and obtain light hydrocarbons, light naphtha, heavy naphtha and hydrogenated heavy oil after separation.

[0047] Furthermore, in the above-mentioned integrated hydrogenation system for producing chemicals from crude oil, as a specific embodiment, the hydrogenated heavy oil obtained from the third fractionation unit enters the second fixed-bed reaction zone through a pipeline.

[0048] Furthermore, in the above-mentioned integrated hydrogenation system for producing chemicals from crude oil, as a specific embodiment, the second fractionation unit is used to receive the second liquid phase feed stream from the second gas-liquid separator, and obtain a second light fraction A, a second light fraction B, a second middle fraction and a second heavy fraction after separation; the second light fraction B is connected to the first ebullated bed reaction zone and / or the second fixed bed reaction zone via a pipeline; the second light fraction A and the second middle fraction enter the second fixed bed reaction zone for treatment.

[0049] Furthermore, in the above-mentioned integrated hydrogenation system for producing crude oil-to-chemicals, as a specific embodiment, the second fixed-bed reaction zone may be equipped with a single fixed-bed reactor, or may be equipped with two or more fixed-bed reactors. Preferably, the two or more fixed-bed reactors are arranged in series, and more preferably, two fixed-bed reactors are arranged in series. When two fixed-bed reactors are used, the first reactor and the second reactor are configured as a refining reactor and a cracking reactor, respectively. The second fixed-bed reaction zone may adopt any of a single-stage series single-pass flow, a single-stage series partial-circulation flow, or a single-stage series full-circulation flow, preferably a single-stage series full-circulation flow.

[0050] Furthermore, in the above-mentioned integrated hydrogenation system for producing chemicals from crude oil, as a specific embodiment, the first light fraction obtained by the first fractionation unit is connected to the first fixed-bed reaction zone and enters the first fixed-bed reaction zone for treatment, or is directly mixed with the light naphtha obtained by the third fractionation unit and used as a raw material for producing ethylene in the steam cracking unit.

[0051] Furthermore, in the above-mentioned integrated hydrogenation system for producing chemicals from crude oil, as a specific embodiment, the first fixed-bed reaction zone is provided with more than one fixed-bed reactor, and a one-pass process can be adopted.

[0052] Furthermore, in the above-mentioned integrated hydrogenation system for producing chemicals from crude oil, as a specific embodiment, a single ebullated bed reactor is provided in the first ebullated bed reaction zone and the second ebullated bed reaction zone, or more than two ebullated bed reactors may be provided. Preferably, the two or more ebullated bed reactors are arranged in series, and a gas-liquid separator is further provided between the reactors; the ebullated bed reactor may be a reactor with an external circulation cup, or it may be a STRONG ebullated bed reactor with a three-phase separator developed by Sinopec (Dalian) Petrochemical Research Institute.

[0053] Furthermore, in the above-mentioned integrated hydrogenation system for producing chemicals from crude oil, as a specific embodiment, the second heavy fraction from the second fractionation unit can be connected to the first ebullated bed reaction zone and / or the second ebullated bed reaction zone and enter therein for treatment, or can also be discharged to connect to the coking unit, solvent deasphalting unit, POX unit (POX refers to partial oxidation hydrogen production) and used as feed for the unit.

[0054] Furthermore, in the above-mentioned integrated hydrogenation system for producing chemicals from crude oil, as a specific embodiment, the fourth gas phase stream from the fourth gas-liquid separator is connected to a purification device and used as circulating hydrogen after treatment. The purification device generally includes a desulfurization device and a membrane separation device. The hydrogen concentration in the hydrogen-rich gas after membrane separation is generally required to reach more than 95%, and is circulated to each reaction unit for use as circulating hydrogen after being pressurized by a circulating hydrogen compressor.

[0055] Furthermore, in the above-mentioned integrated hydrogenation system for producing chemicals from crude oil, as a specific embodiment, the outlet of the circulating hydrogen compressor is connected to the first gas-liquid separator and the second gas-liquid separator via pipelines respectively.

[0056] Compared with the prior art, the integrated crude oil-to-chemicals hydrogenation process and hydrogenation system provided by the present invention have the following advantages:

[0057] (1) In the integrated hydrogenation process and hydrogenation system for producing crude oil-based chemicals provided by the present invention, the ebullated bed reaction zone and the fixed bed reaction zone are efficiently coupled and integrated, and the gas phase components after the reaction in the ebullated bed reaction zone are directly sent to the subsequent fixed bed reaction zone, which can fully utilize the pressure level of the ebullated bed reaction zone and save operating costs. By introducing circulating hydrogen into the gas-liquid separator, especially the gas-liquid separator between the ebullated bed reactors, the light fraction is separated into the gas phase material by using circulating hydrogen, and the impurities are removed by combining with the added high-pressure first fixed bed reaction zone, and the high-fraction gas phase is directly fed into the second fixed bed reaction zone again for use as a hydrogen raw material. In the entire process flow setting, hot feeding is realized between each hydrogenation unit, eliminating the heating furnace, high-pressure pump and other equipment of each individual hydrogenation unit. At the same time, each hydrogenation unit shares a common fractionation system, circulating hydrogen desulfurization tower and other equipment, which greatly reduces the equipment investment and energy consumption.

[0058] (2) Based on the theory of dynamic equilibrium of reaction, free radical reaction and carbonium ion reaction mechanism, the present invention introduces the second light fraction B (mainly heavy diesel fraction) into the first ebullated bed reaction zone under the premise of fully understanding the reaction equilibrium conversion process mechanism of the ebullated bed reaction zone, so that the conversion balance of the raw material to the light fraction changes, the equilibrium conversion rate of the raw material to the wax oil fraction and the naphtha fraction increases, and the chemical yield can be improved. After analysis, it is believed that on the one hand, it is more difficult to produce naphtha by hydrocracking the diesel fraction in the fixed bed relative to the wax oil fraction; on the other hand, with the introduction of the diesel fraction, a larger proportion of the raw material is converted into the wax oil fraction, and the entire raw material colloidal structure can maintain a high stability; on the third hand, because the ebullated bed reaction zone is mainly thermal cracking of free radical reaction, and the fixed bed reaction zone is mainly catalytic cracking of carbonium ion reaction, the light oil yield can be reduced as much as possible under the premise of ensuring the conversion rate, so as to avoid the generation of a large amount of methane C1 components and improve the effective yield of chemicals.

[0059] (3) The present invention is based on the mass transfer kinetics and hydrogen dissolution equilibrium theory. Compared with the direct introduction of residual oil raw materials into the boiling bed, the introduction of light components increases the diffusion of residual oil macromolecules into the catalyst pores, promoting the removal of impurities such as sulfur, nitrogen, and metals. At the same time, compared with the residual oil system, the light fraction has a higher solubility in hydrogen, which can quickly replenish the hydrogen reacted in the system, accelerate the reaction, slow down coking, and significantly improve the properties of hydrogenated heavy oil. BRIEF DESCRIPTION OF THE DRAWINGS

[0060] Figure 1 The figure is a schematic diagram of the integrated hydrogenation process flow for producing chemicals from crude oil according to one embodiment of the present invention.

[0061] Wherein, 1-crude oil; 2-first fractionation unit; 3-first light fraction; 4-first middle fraction; 5-first heavy fraction; 6-first ebullated bed reaction zone; 7-reaction product of the first ebullated bed reaction zone; 8-first gas-liquid separator; 9-first gas-phase stream; 10-first liquid-phase stream; 11-second ebullated bed reaction zone; 12-reaction product of the second ebullated bed reaction zone; 13-second gas-liquid separator; 14-second gas-phase stream; 15-second liquid-phase stream; 16-second fractionation unit; 17-second light fraction; 18-second middle fraction; 19-second heavy fraction; 20-first Fixed-bed reaction zone; 21-reaction product of the first fixed-bed reaction zone; 22-third gas-liquid separator; 23-third gas-phase feed stream; 24-third liquid-phase feed stream; 25-first reactor of the second fixed-bed reaction zone; 26-second reactor of the second fixed-bed reaction zone; 27-product of the second fixed-bed reaction zone; 28-fourth gas-liquid separator; 29-fourth gas-phase feed stream; 30-fourth liquid-phase feed stream; 31-third fractionation unit; 32-light hydrocarbons; 33-light naphtha; 34-heavy naphtha; 35-hydrogenated heavy oil; 36-circulating hydrogen compressor; 37-circulating hydrogen; 38-new hydrogen.

[0062] Figure 2 This is a schematic diagram of the integrated hydrogenation process flow for producing chemicals from crude oil according to another embodiment of the present invention.

[0063] Wherein: 1-crude oil; 2-first fractionation unit; 3-first light fraction; 4-first middle fraction; 5-first heavy fraction; 6-first ebullated bed reaction zone; 7-reaction product of the first ebullated bed reaction zone; 8-first gas-liquid separator; 9-first gas-phase stream; 10-first liquid-phase stream; 11-second ebullated bed reaction zone; 12-reaction product of the second ebullated bed reaction zone; 13-second gas-liquid separator; 14-second gas-phase stream; 15-second liquid-phase stream; 16-second fractionation unit; 17-second light fraction A; 18-second middle fraction; 19-second heavy fraction; 20-first fixed bed reaction zone; reaction zone; 21-reaction product of the first fixed-bed reaction zone; 22-third gas-liquid separator; 23-third gas-phase feed stream; 24-third liquid-phase feed stream; 25-first reactor of the second fixed-bed reaction zone; 26-second reactor of the second fixed-bed reaction zone; 27-product of the second fixed-bed reaction zone; 28-fourth gas-liquid separator; 29-fourth gas-phase feed stream; 30-fourth liquid-phase feed stream; 31-third fractionation unit; 32-light hydrocarbons; 33-light naphtha; 34-heavy naphtha; 35-hydrogenated heavy oil; 36-circulating hydrogen compressor; 37-circulating hydrogen; 38-new hydrogen; 39-second light fraction B.

[0064] Figure 3 Schematic diagram of the process flow of a comparative example of the present invention. DETAILED DESCRIPTION

[0065] Next, the technical features of the present invention will be further described through embodiments and in conjunction with the accompanying drawings, but these embodiments are not intended to limit the present invention.

[0066] Unless expressly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising” will be understood to include the stated elements or components but not to exclude other elements or components.

[0067] In this document, for ease of description, spatially relative terms such as "below," "beneath," "down," "above," "above," etc. may be used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that the spatially relative terms are intended to encompass different orientations of an object in use or operation in addition to the orientation depicted in the drawings. For example, if the object in the figure is turned over, the element described as being "below" or "below" other elements or features will be oriented "above" the element or feature. Therefore, the exemplary term "below" can include both below and above directions. Objects may also have other orientations (rotated 90 degrees or other orientations) and the spatially relative terms used herein should be interpreted accordingly.

[0068] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit specific positions or relative relationships. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable with each other.

[0069]

[0046] All numerical values ​​for parameters (eg, amounts or conditions) herein are to be understood as being modified in all instances by the term "about," whether or not "about" actually precedes the numerical value.

[0070] like Figure 1As shown, the present invention provides an integrated hydrogenation process for producing chemicals from crude oil. Crude oil 1 first enters a first fractionation unit 2, and after separation, a first light fraction 3, a first middle fraction 4, and a first heavy fraction 5 are obtained. The first heavy fraction 5 enters a first ebullated bed reaction zone 6, and is contacted with recycled hydrogen 37 and new hydrogen 38 for reaction. The reaction product 7 obtained in the first ebullated bed reaction zone after the reaction enters a first gas-liquid separator 8, and after separation, a first gas phase stream 9 and a first liquid phase stream 10 are obtained. The first liquid phase stream 10 enters The second ebullated bed reaction zone 11 contacts the recycled hydrogen 37 and the new hydrogen 38 to react. The reaction product 12 of the second ebullated bed reaction zone obtained after the reaction enters the second gas-liquid separator 13, and after separation, a second gas phase stream 14 and a second liquid phase stream 15 are obtained. The second gas phase stream 14, the first light fraction 3 and the first gas phase stream 9 enter the first fixed bed reaction zone 20. The reaction product 21 of the first fixed bed reaction zone obtained after the reaction enters the third gas-liquid separator 22, and is further separated into the third gas phase stream 14 and the second liquid phase stream 15. The second liquid phase stream 15 enters the second fractionation unit 16, and after separation, a second light fraction 17, a second middle fraction 18, and a second heavy fraction 19 are obtained; wherein the second light fraction 17, the second middle fraction 18, the first middle fraction 4 and the third gas phase stream 23 enter the first reactor 25 of the second fixed bed reaction zone and the second reactor 26 of the second fixed bed reaction zone in sequence, and are contacted with the new hydrogen 38 for reaction, and the product material 2 of the second fixed bed reaction zone is obtained after the reaction. 7 enters the fourth gas-liquid separator 28 to obtain a fourth gas-phase stream 29 and a fourth liquid-phase stream 30. The fourth gas-phase stream 29 passes through a hydrogen purification and recovery system (not shown in the figure) and enters a circulating hydrogen compressor 36 for compression to obtain circulating hydrogen 37. The fourth liquid-phase stream 30 and the third liquid-phase stream 24 enter the third fractionation unit 31 and are separated into light hydrocarbons 32, light naphtha 33, heavy naphtha 34 and hydrogenated heavy oil 35. The hydrogenated heavy oil 35 is returned to the first reactor 25 of the second fixed-bed reaction zone for processing.

[0071] like Figure 2 As shown, another integrated hydrogenation process for producing chemicals from crude oil provided by the present invention is Figure 1 The process flow is essentially the same, except that the second liquid stream 15 enters the second fractionation unit 16, where it is separated to produce a second light fraction A17, a second light fraction B39, a second middle fraction 18, and a second heavy fraction 19. The second light fraction B39 can be fully or partially returned to the first ebullated-bed reaction zone 6 for treatment. The second light fraction A17 sequentially enters the first reactor 25 and the second reactor 26 of the second fixed-bed reaction zone for treatment.

[0072] In this paper, the ebullated bed reactor adopts the STRONG ebullated bed reactor with built-in three-phase separator developed by Sinopec (Dalian) Petrochemical Research Institute Co., Ltd.

[0073] In this article, the properties of crude oil used in the examples and comparative examples are shown in Table 1.

[0074] Table 1 Crude oil properties

[0075]

[0076]

[0077] Example 1

[0078] Example 1 uses Figure 1 In the process flow shown, crude oil is separated by the first fractionation unit to obtain a first light fraction, a first middle fraction and a first heavy fraction, wherein the cut point temperature between the first light fraction and the first middle fraction is 160°C, and the cut point temperature between the first middle fraction and the first heavy fraction is 340°C.

[0079] The first ebullated bed reaction zone and the second ebullated bed reaction zone adopt a dual-reactor series mode. The catalyst loaded in the first ebullated bed reaction zone is FEM-10 ebullated bed hydrogenation catalyst, and the catalyst loaded in the second ebullated bed reaction zone is FES-31 ebullated bed hydrogenation catalyst. The reaction pressure of the first ebullated bed reaction zone and the second ebullated bed reaction zone is 15MPa, the hydrogen-to-oil volume ratio is 500, and the total volume space velocity of the ebullated bed is 0.20h -1 The reaction temperature of the first ebullated bed reaction zone is 422°C, and the reaction temperature of the second ebullated bed reaction zone is 429°C.

[0080] The first fixed bed reaction zone is filled with FC-32 hydrocracking catalyst and FF-12 hydrorefining catalyst. The reaction conditions of the first fixed bed reaction zone are: reaction pressure 16MPa, reaction temperature 350℃, volume space velocity 1.8h -1 , the hydrogen-to-oil volume ratio is 1300.

[0081] The cutting temperature of the second light fraction and the second middle fraction is 365°C, and the cutting temperature of the second middle fraction and the second heavy fraction is 520°C.

[0082] The first reactor in the second fixed-bed reaction zone is filled with FF-56 pretreatment catalyst, and the second reactor is filled with FC-76 hydrocracking catalyst and FF-34 hydrofining catalyst. The reaction conditions of the first reactor in the second fixed-bed reaction zone are: reaction pressure of 16.0 MPa, reaction temperature of 368°C, volume space velocity of 1.4 h -1, the hydrogen-oil volume ratio is 800; the reaction conditions of the second reactor are: reaction pressure of 16.0 MPa, reaction temperature of 380 ° C, volume space velocity of 2.0 h -1 , the hydrogen-to-oil volume ratio is 1000.

[0083] Example 2

[0084] Example 2 uses Figure 2 The process flow is essentially the same as that of Example 1, except that the second liquid phase stream enters the second fractionation unit, where it is separated to produce a second light fraction A, a second light fraction B, a second middle fraction, and a second heavy fraction. The second light fraction B is returned to the first ebullated bed reaction zone 6 for treatment, and the second light fraction B accounts for 10% of the total feed to the first ebullated bed reaction zone. Other process parameters are as follows:

[0085] After the crude oil is separated by the first fractionation unit, a first light fraction, a first middle fraction and a first heavy fraction are obtained, wherein the cut point between the first light fraction and the first middle fraction is 200°C, and the cut point between the first middle fraction and the first heavy fraction is 370°C.

[0086] The first ebullated bed reaction zone and the second ebullated bed reaction zone adopt a dual-reactor series mode. The catalyst loaded in the first ebullated bed reaction zone is FEM-10 ebullated bed hydrogenation catalyst, and the catalyst loaded in the second ebullated bed reaction zone is FES-31 ebullated bed hydrogenation catalyst. The reaction pressure of the first ebullated bed reaction zone and the second ebullated bed reaction zone is 18MPa, the hydrogen-to-oil volume ratio is 700, and the total volume space velocity of the ebullated bed is 0.27h -1 The reaction temperature of the first ebullated bed reaction zone is 424°C, and the reaction temperature of the second ebullated bed reaction zone is 430°C.

[0087] The first fixed bed reaction zone is filled with FC-76 hydrocracking catalyst and FF-12 hydrorefining catalyst. The reaction conditions of the first fixed bed reaction zone are: reaction pressure 17MPa, reaction temperature 350℃, volume space velocity 1.8h -1 , the hydrogen-to-oil volume ratio is 1300.

[0088] The cutting temperature of the second light fraction A and the second light fraction B is 280°C, the cutting temperature of the second light fraction B and the second middle fraction is 360°C, and the cutting temperature of the second middle fraction and the second heavy fraction is 520°C.

[0089] The first reactor in the second fixed-bed reaction zone is filled with FF-66 pretreatment catalyst, and the second reactor is filled with FC-76 hydrocracking catalyst and FF-12 hydrofining catalyst. The reaction conditions of the first reactor in the second fixed-bed reaction zone are: reaction pressure of 16.0 MPa, reaction temperature of 360°C, volume space velocity of 1.2 h -1, the hydrogen-oil volume ratio is 800; the reaction conditions of the second reactor are: reaction pressure of 16.0 MPa, reaction temperature of 385 ° C, volume space velocity of 2.2 h -1 , the hydrogen-to-oil volume ratio is 1000.

[0090] Example 3

[0091] Example 3 uses the same process flow as Example 2, except that the process conditions are adjusted. Other process parameters are as follows:

[0092] The second light fraction B is returned to the first ebullated-bed reaction zone 6 for processing. The second light fraction B comprises 10% of the total feed to the first ebullated-bed reaction zone. The crude oil is separated by the first fractionation unit to produce a first light fraction, a first middle fraction, and a first heavy fraction. The cut point between the first light fraction and the first middle fraction is 200°C, while the cut point between the first middle fraction and the first heavy fraction is 370°C.

[0093] The first ebullated bed reaction zone and the second ebullated bed reaction zone adopt a dual-reactor series mode. The catalyst loaded in the first ebullated bed reaction zone is FEM-10 ebullated bed hydrogenation catalyst, and the catalyst loaded in the second ebullated bed reaction zone is FES-31 ebullated bed hydrogenation catalyst. The reaction pressure of the first ebullated bed reaction zone and the second ebullated bed reaction zone is 17MPa, the hydrogen-to-oil volume ratio is 400, and the total volume space velocity of the ebullated bed is 0.25h -1 The reaction temperature of the first ebullated bed reaction zone is 421°C, and the reaction temperature of the second ebullated bed reaction zone is 428°C.

[0094] The first fixed bed reaction zone is filled with FC-76 hydrocracking catalyst and FF-12 hydrorefining catalyst. The reaction conditions of the first fixed bed reaction zone are: reaction pressure 16MPa, reaction temperature 370℃, volume space velocity 1.8h -1 , the hydrogen-to-oil volume ratio is 1000.

[0095] The cutting temperature of the second light fraction A and the second light fraction B is 320°C, the cutting temperature of the second light fraction B and the second middle fraction is 370°C, and the cutting temperature of the second middle fraction and the second heavy fraction is 520°C.

[0096] The first reactor in the second fixed-bed reaction zone is filled with FF-66 pretreatment catalyst, and the second reactor is filled with FC-76 hydrocracking catalyst and FF-12 hydrofining catalyst. The reaction conditions of the first reactor in the second fixed-bed reaction zone are: reaction pressure of 15.0 MPa, reaction temperature of 350°C, volume space velocity of 1.0 h -1 , the hydrogen-oil volume ratio is 1000; the reaction conditions of the second reactor are: reaction pressure of 15.0 MPa, reaction temperature of 380 ° C, volume space velocity of 1.8 h-1 , the hydrogen-to-oil volume ratio is 1300.

[0097] Comparative Example 1

[0098] Figure 3 This is the process flow chart used in Comparative Example 1. Crude oil 1 is separated by the atmospheric and vacuum unit 2 to obtain straight-run naphtha 3, straight-run diesel 4, straight-run wax oil 5 and vacuum residue 6, wherein the straight-run naphtha 3 and the hydrogen at the outlet of the first compressor 10 are mixed and enter the first fixed-bed reaction zone 7, and the generated oil enters the first gas-liquid separation unit 8. The liquid phase flow obtained after separation enters the first fractionation unit 9, and after separation, the first light hydrocarbons 11, the first light naphtha 12 and the first heavy naphtha 13 are obtained; the straight-run diesel 4 and the hydrogen at the outlet of the second compressor 21 are mixed and enter the second fixed-bed reaction zone 14, and the generated oil enters The liquid phase stream obtained after separation in the second gas-liquid separation unit 15 enters the second fractionation unit 16 for separation to obtain the second light hydrocarbon 17, the second light naphtha 18, the second heavy naphtha 19 and the second heavy fraction 20, wherein the second heavy fraction 20 is all recycled to the second fixed bed reaction zone 14; the straight run wax oil 5 is mixed with the hydrogen at the outlet of the third compressor 25 and sequentially enters the first reactor 22 and the second reactor 23 arranged in series in the third fixed bed reaction zone for reaction, and the generated oil enters the third gas-liquid separation unit 24 for separation to obtain the liquid phase stream which enters the third fractionation unit 26 for separation to obtain To the third light hydrocarbon 27, the third light naphtha 28, the third heavy naphtha 29 and the third heavy fraction 30, wherein the third heavy fraction 30 is all circulated to the first reactor 22 of the third fixed bed reaction zone; the vacuum residue 6 is mixed with the hydrogen at the outlet of the fourth compressor 36 and enters the first ebullated bed reactor 31 of the ebullated bed reaction zone, the product flow enters the fourth gas-liquid separation unit 32, and the liquid phase after separation enters the second ebullated bed reactor 33 of the ebullated bed reaction zone, the reaction product and the gas phase separated by the fourth gas-liquid separation unit 32 enter the fifth gas-liquid separation unit 34 together, and the gas phase obtained after separation After entering the sixth gas-liquid separation unit 35, the gas phase logistics is obtained and enters the compressor system 36. The liquid phase logistics of the fifth gas-liquid separation unit 34 and the liquid phase logistics of the sixth gas-liquid separation unit 35 enter the fourth fractionation unit 37 for separation to obtain boiling bed naphtha 38, boiling bed diesel 39, boiling bed wax oil 40 and boiling bed hydrogenated heavy oil 41, among which the boiling bed naphtha 38 enters the first fixed bed reaction zone 7 for processing, the boiling bed diesel 39 enters the second fixed bed reaction zone 14 for processing, and the boiling bed wax oil enters the first reactor 22 and the second reactor 23 in the third fixed bed reaction zone for processing.

[0099] The first fixed bed reaction zone was filled with FH-40B commercial grade catalyst. The reaction conditions were: reaction temperature 300°C, reaction pressure 2.4 MPa, volume space velocity 8.0 h -1 , hydrogen to oil volume ratio 100;

[0100] The second fixed bed reaction zone was filled with FF-66 and FC-32 hydrogenation catalysts in the direction of liquid material flow. The reaction conditions were: reaction temperature 365 ° C, reaction pressure 14.0 MPa, reaction space velocity 1.6 h -1 , hydrogen to oil volume ratio is 1000.

[0101] The third fixed bed reaction zone unit was filled with FF-56 and FC-76 hydrogenation catalysts in the direction of liquid phase material flow. The reaction conditions were: reaction temperature 385 ° C, reaction pressure 16.0 MPa, reaction space velocity 1.8 h -1 , hydrogen to oil volume ratio is 1000.

[0102] The ebullated bed reaction zone was filled with FEM-10 and FES-31 hydrogenation catalysts in the direction of liquid material flow. The reaction conditions were: reaction temperature 425 ° C, reaction pressure 17.0 MPa, reaction space velocity 0.18 h -1 , hydrogen to oil volume ratio 500.

[0103] The comparison results of Examples 1-3 and Comparative Example 1 are shown in Tables 2 and 3.

[0104] Table 2 Product distribution

[0105]

[0106] Table 3 Properties of Hydrogenated Heavy Oil

[0107]

[0108]

Claims

1. An integrated hydrogenation process for producing crude oil-based chemicals, the hydrogenation process comprising the following steps: (1) Under separation conditions, the crude oil is separated to obtain a first light fraction, a first middle fraction, and a first heavy fraction; the cutting temperature of the first light fraction and the first middle fraction is 60 to 230°C; the cutting temperature of the first middle fraction and the first heavy fraction is 145 to 400°C; (2) The first heavy fraction obtained in step (1) enters the first ebullated bed reaction zone, contacts with hydrogen and reacts, and the reaction products are separated to obtain a first gas phase stream and a first liquid phase stream; (3) The first liquid stream obtained in step (2) enters the second ebullated bed reaction zone, contacts with hydrogen for reaction, and the reaction products are separated to obtain a second gas stream and a second liquid stream, and the second liquid stream is separated to obtain a second light fraction A, a second light fraction B, a second middle fraction, and a second heavy fraction; wherein all or part of the second light fraction B is recycled to the first ebullated bed reaction zone for treatment; the cutting temperature of the second light fraction A and the second light fraction B is 210-330°C; the cutting temperature of the second light fraction B and the second middle fraction is 300-400°C; and the cutting temperature of the second middle fraction and the second heavy fraction is 480-550°C; (4) The first gas-phase stream obtained in step (2) and the second gas-phase stream obtained in step (3) enter the first fixed-bed reaction zone, contact with hydrogen to react, and the reaction products are separated to obtain a third gas-phase stream and a third liquid-phase stream; (5) The first middle distillate obtained in step (1), the second light fraction A obtained in step (3), the second middle distillate obtained in step (3), and the third gaseous phase stream obtained in step (4) enter the second fixed bed reaction zone, contact with hydrogen to react, and the reaction products are separated to obtain a fourth gaseous phase stream and a fourth liquid phase stream; (6) The third liquid phase stream obtained in step (4) and the fourth liquid phase stream obtained in step (5) are mixed and separated to obtain light hydrocarbons, light naphtha, heavy naphtha and hydrogenated heavy oil.

2. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The separation in step (1) is carried out by any one of flash distillation, atmospheric distillation and atmospheric / reduced pressure distillation.

3. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The cutting temperature of the first light fraction and the first middle fraction in step (1) is 65-200°C; the cutting temperature of the first middle fraction and the first heavy fraction is 175-380°C.

4. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction conditions of the first ebullated bed reaction zone are as follows: reaction temperature of 350-450°C, reaction pressure of 10.0-19.0 MPa, hydrogen-to-oil volume ratio of 300-1000, liquid hourly volume space velocity of 0.1-3.0 h -1 .

5. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction conditions of the first ebullated bed reaction zone are as follows: reaction temperature of 380-430°C, reaction pressure of 13.0-18.0 MPa, hydrogen-to-oil volume ratio of 400-600, liquid hourly volume space velocity of 0.15-1.0 h -1 .

6. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction conditions of the second ebullated bed reaction zone are as follows: reaction temperature of 350-450°C, reaction pressure of 10.0-19.0 MPa, hydrogen-to-oil volume ratio of 300-1000, liquid hourly volume space velocity of 0.1-3.0 h -1 .

7. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction conditions of the second ebullated bed reaction zone are as follows: reaction temperature of 380-430°C, reaction pressure of 13.0-18.0 MPa, hydrogen-to-oil volume ratio of 400-600, liquid hourly volume space velocity of 0.15-1.0 h -1 .

8. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The cutting temperature of the second middle distillate and the second heavy distillate is 500-540°C.

9. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: When part of the second light fraction B is recycled back to the first ebullated-bed reaction zone for treatment, the remaining part enters the second fixed-bed reaction zone for treatment.

10. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The cutting temperature of the second light fraction A and the second light fraction B is 240-330°C; the cutting temperature of the second light fraction B and the second middle fraction is 350-380°C.

11. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction conditions of the first fixed bed reaction zone are as follows: reaction temperature of 280-350°C, reaction pressure of 10-19 MPa, hydrogen-to-oil volume ratio of 500-1200, liquid hourly volume space velocity of 0.5-3.0 h -1 .

12. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction conditions of the first fixed bed reaction zone are as follows: reaction temperature of 300-330°C, reaction pressure of 13-18 MPa, hydrogen-to-oil volume ratio of 700-1000, liquid hourly volume space velocity of 1.0-2.0 h -1 .

13. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction conditions of the second fixed bed reaction zone are as follows: reaction temperature is 350-400°C, hydrogen to oil volume ratio is 700-1500, liquid hourly volume space velocity is 0.5-3.0h -1 , the reaction pressure is 12.0~16.0MPa.

14. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction conditions of the second fixed bed reaction zone are as follows: reaction temperature is 360-390°C, hydrogen-to-oil volume ratio is 800-1200, liquid hourly volume space velocity is 1.0-2.0h -1 , the reaction pressure is 13.0~15.0MPa.

15. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The first light fraction obtained in step (1) enters the first fixed bed reaction zone for treatment, or is directly mixed with the light naphtha obtained in step (6) without hydrogenation treatment and used as a raw material for the steam cracking unit to produce ethylene.

16. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The second heavy fraction in step (3) is recycled to the first ebullated bed reaction zone and / or the second ebullated bed reaction zone for treatment, or discharged as a feedstock for a coking, solvent deasphalting, or partial oxidation hydrogen production unit.

17. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The fourth gas phase stream in step (5) is used as circulating hydrogen after purification.

18. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction product in step (2) is separated to obtain a first gas phase stream and a first liquid phase stream. During the separation, recycled hydrogen and / or new hydrogen are introduced as a stripping medium to separate the reaction product together.

19. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The reaction product in step (3) is separated to obtain a second gas phase stream and a second liquid phase stream. During the separation, recycled hydrogen and / or new hydrogen are introduced as a stripping medium to separate the reaction product together.

20. The integrated hydrogenation process for producing chemicals from crude oil according to claim 1, characterized in that: The hydrogenated heavy oil in step (6) is circulated back to the second fixed bed reaction zone for treatment.

21. An integrated hydrogenation system for producing crude oil-to-chemicals for implementing the integrated hydrogenation process for producing crude oil-to-chemicals according to any one of claims 1 to 20, the system comprising a first fractionation unit, a first ebullated bed reaction zone, a first gas-liquid separator, a second ebullated bed reaction zone, a second gas-liquid separator, a first fixed bed reaction zone, a second fixed bed reaction zone, a second fractionation unit, a third gas-liquid separation unit, a fourth gas-liquid separator, and a fourth fractionation unit; a first fractionation unit, which is used to receive and separate crude oil, and obtain a first light fraction, a first middle fraction and a first heavy fraction after the crude oil is separated; a first ebullated bed reaction zone, which is used to receive the first heavy fraction from the first fractionation unit and contact it with hydrogen to react; a first gas-liquid separator, which is used to receive and separate the reaction product from the first ebullated bed reaction zone to obtain a first gas phase material flow and a first liquid phase material flow after separation; a second ebullated bed reaction zone, which is used to receive the first liquid phase stream from the first gas-liquid separator and contact it with hydrogen to react; a second gas-liquid separator, which is used to receive the reaction product from the second ebullated bed reaction zone and obtain a second gas phase material flow and a second liquid phase material flow after separation; a second fractionation unit, which is used to receive the second liquid phase stream from the second gas-liquid separator and obtain a second light fraction A, a second light fraction B, a second middle fraction and a second heavy fraction after separation; The second light fraction B is connected to the first ebullated bed reaction zone and / or the second fixed bed reaction zone via a pipeline; the second light fraction A and the second middle fraction enter the second fixed bed reaction zone for treatment; a first fixed bed reaction zone, which is used to receive the first gas-phase material flow from the first gas-liquid separator and the second gas-phase material flow from the second gas-liquid separator, and contact them with hydrogen to react; a third gas-liquid separator, which is used to receive the reaction product from the first fixed bed reaction zone and obtain a third gas phase material flow and a third liquid phase material flow after separation; a second fixed-bed reaction zone, which is used to receive the first middle distillate from the first fractionation unit, the second light fraction and the second middle distillate from the second fractionation unit, and the third gaseous stream from the third separator, and contact them with hydrogen for reaction; a fourth gas-liquid separator, which is used to receive the reaction product from the second fixed-bed reaction zone and obtain a fourth gas phase material flow and a fourth liquid phase material flow after separation; The third fractionation unit is used to receive the third liquid phase stream from the third gas-liquid separation unit and the fourth liquid phase stream from the fourth gas-liquid separator, and obtain light hydrocarbons, light naphtha, heavy naphtha and hydrogenated heavy oil after separation.

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