Hydroconversion process of heavy and medium hydrocarbons using hydrogen in three stages in series

Abstract

A combined hydroconversion process of heavy hydrocarbons, medium hydrocarbons using tertiary series hydrogen, hydrogen-rich gas is used in the first hydrogenation reaction process R1, such as slurry bed hydrocracking process, the product R1P obtained in the first hot high pressure separation process S1 is separated into hot high pressure gas S1V and hot high pressure liquid S1L, S1V is subjected to the second hydrogenation reaction process R2, such as ebullated bed hydrocracking process, of medium hydrocarbons, such as coal tar distillate oil, the product R2P obtained in the second hot high pressure separation process S2 is separated into hot high pressure gas S2V and hot high pressure liquid S2L, which is usually hydrogenated cracking raw material hydrocarbon, S2V is subjected to the third hydrogenation reaction process R3, such as fixed bed hydrogenation process, the product R3P obtained in the third separation process S3 is separated into hydrogen-rich third separation gas S3V and third hydrogenation oil S3L, at least part of S3V is recycled to R1 and / or R2 and / or R3; the distillate oil obtained by separating S1L can enter R2 and / or R3.

Description

TECHNICAL FIELD

[0001] The present application relates to a combined hydrogenation conversion method of heavy hydrocarbon and medium hydrocarbon by using hydrogen in three stages in series, which is suitable for the classification and combined hydrogenation conversion of large-scale medium and low temperature coal tar. BACKGROUND

[0002] The present application aims to provide an efficient combined hydrogenation conversion method of heavy hydrocarbon and medium hydrocarbon, and one application object is the classification and combined hydrogenation conversion of large-scale medium and low temperature coal tar, so as to simplify the process, reduce investment, reduce energy consumption, improve heavy oil conversion rate, and produce more naphtha, and it is particularly suitable for capacity expansion and modification of existing devices. In the known hydrogenation conversion mode, the suspended bed hydrogenation reaction process, especially the suspended bed hydrogenation reaction process using molybdenum-based suspended bed hydrogenation catalyst, can realize deep hydrogenation cracking of coal pitch components with high selectivity, which has high conversion rate and high selectivity that the boiling bed hydrogenation reaction process cannot achieve. However, this does not mean that the boiling bed hydrogenation reaction process cannot be used to process coal tar-based hydrocarbon streams containing coal pitch components.

[0003] On the other hand, the boiling bed hydrogenation reaction process with liquid product circulation reaction mode can conduct the reaction heat of the boiling bed hydrogenation process to the reaction raw oil, so as to reduce the preheating temperature of the hydrogenation reaction raw oil, reduce the heat exchanger and heating furnace investment, reduce the fuel consumption, reduce the amount of circulating hydrogen, in one word, it contains the hydrogenation conversion capacity with a certain sense of "local process self-consistency", so that the change range brought by the original device process can be reduced, which is beneficial to reduce the investment and shorten the modification period of the existing device. The newly added boiling bed hydrogenation reaction system can be constructed in advance, and connected with the original system through the change and addition of the pipeline system.

[0004] The existing product scheme of coal tar hydrogenation mainly produces diesel blending components is facing the change of adjusting to produce more naphtha fraction, so the proportion of naphtha in the product of coal tar hydrogenation cracking reaction will increase, and because the boiling point of naphtha component is lower, the product of coal tar hydrogenation cracking reaction can be separated in a hot high-pressure separator (such as a TS4 with additional hydrogen stripping) with a proper high operating temperature into a hot high-vapor TS4V rich in naphtha components and a hot high-liquid TS4L from which most of the naphtha components are removed, and then at least part of the hydrocarbon stream based on the hot high-liquid TS4L is returned to the coal tar hydrogenation cracking reaction process R4 as a high-pressure recycle oil TS4LR for short-path selective hydrogenation cracking reaction, so as to reduce the amount of coal tar hydrogenation cracking oil that needs to be treated in the hydrogenation cracking oil fractionation process, facilitate the expansion and modification of the hydrogenation cracking oil fractionation process by eliminating the bottleneck, and at the same time, the operating temperature of the hot high-pressure separator TS4 can be increased to increase the heat energy of the hot high-liquid TS4L entering the fractionation process, and the heat supply of the fractionation process is reduced; at the same time, on the one hand, part of the high-pressure recycle oil TS4LR returns to the inlet of the front catalyst bed of the fourth hydrogenation reaction process R4 as a heat carrier, and on the other hand, part of the high-pressure recycle oil TS4LR can be cooled by a heat exchanger that preheats the fractionation process materials and then returned to the inlet of the rear catalyst bed of the fourth hydrogenation reaction process R4 as a cooling medium to reduce the amount of quenching recycle hydrogen.

[0005] For the hot high-vapor treatment system of the existing or newly added suspended bed hydrogenation reaction process, these hydrogen resources can be used for the hydrofining of distillate oil, especially low-boiling distillate oil, without going through the hydrogenation cracking process, so as to avoid the secondary hydrogenation cracking of low-carbon conventional liquid hydrocarbons with a carbon number less than 12, and facilitate the improvement of liquid yield and the reduction of hydrogen consumption.

[0006] Similarly, for the hot high-vapor treatment system of the existing or newly added boiling bed hydrogenation reaction process, these hydrogen resources can be used for the hydrofining of distillate oil, especially low-boiling distillate oil, without going through the hydrogenation cracking process, so as to avoid the secondary hydrogenation cracking of low-carbon conventional liquid hydrocarbons with a carbon number less than 12, and facilitate the improvement of liquid yield and the reduction of hydrogen consumption.

[0007] For the coal tar hydrogenation cracking reaction process, in order to improve the activity of the catalyst (including hydrogenation cracking catalyst, hydrofining catalyst), especially the working condition of hydrogenation cracking for producing more naphtha, the concentration of basic component ammonia in the gas phase of the reaction process needs to be controlled, therefore, at least most of the ammonia gas needs to be removed before the distillate hydrofining reaction product enters the hydrogenation cracking reaction process, which requires a separation process of the distillate hydrofining reaction product, the simplest way of which is to use only a hot high-pressure separation process to remove ammonia, and then the hot high-liquid from which the ammonia is removed enters the hydrogenation cracking reaction process in a high-pressure state.

[0008] Based on the above analysis, the present application proposes a combined process, which is particularly suitable for the capacity expansion and modification of existing devices.

[0009] The basic idea of the present application is that the combined hydroconversion process of heavy hydrocarbon and medium hydrocarbon using hydrogen in three stages in series, the hydrogen-rich gas is separated into hot high-pressure gas S1V and hot high-pressure liquid S1L by separating the product R1P obtained in the first hydrogenation reaction process R1 such as slurry bed hydrocracking process of coal pitch in the first hot high-pressure separation process S1, S1V is separated into hot high-pressure gas S2V and hot high-pressure liquid S2L which is usually used as the hydrocracking raw material hydrocarbon by separating the product R2P obtained in the second hydrogenation reaction process R2 such as ebullated bed hydrocracking process of medium hydrocarbon such as coal tar distillate oil in the second hot high-pressure separation process S2, S2V is separated into hydrogen-rich third separation gas S3V and third hydrogenation product oil S3L by separating the product R3P obtained in the third hydrogenation reaction process R3 such as fixed bed hydrocracking process in the third separation process S3, and at least part of S3V is recycled to R1 and / or R2 and / or R3; the distillate oil obtained by separating S1L can enter R2 and / or R3. Usually, the fourth hydrogenation product R4P obtained by completing the hydrocracking reaction of S2L in the fourth hydrogenation reaction process R4 such as fixed bed hydrocracking process is separated into fourth gas S4V and fourth liquid S4L in the fourth hot high-pressure separation process S4; the separation process of part or all of the third liquid S3L and part or all of the fourth liquid S4L can be partially or completely combined; the fourth hydrogenation product R4P is separated into hot high-pressure gas TS4V rich in naphtha components and hot high-pressure oil TS4L in the hot high-pressure separation part TS4 which can exist in the stripping hydrogen gas, and at least part of the hydrogen stream based on the hot high-pressure oil TS4L is returned to the fourth hydrogenation reaction process R4 for short-flow selective hydrocracking reaction, so that the number of fourth hydrogenation product oils processed can be reduced, and the load of the fractionation process thereof can be reduced. Chinese patent ZL200610071230.2 discloses a coal tar hydroconversion method, in which the coal tar raw material is converted into first reaction effluent in the first reaction part, the first reaction effluent is separated into first hot high-pressure oil in the first hot high-pressure separation part; and the first hot high-pressure oil is converted into second reaction effluent in the second reaction part. The present application provides a hydroconversion method for the utilization of oxygen-rich coal tar and wide distillate coal tar. The functions of the method are: first, the hot high-pressure separation part can remove most of the ammonia gas, water vapor, and part of the low-boiling hydrocarbon components; second, the first reaction product, i.e., the hot high-pressure oil, is directly connected to the high-pressure part of the second reaction part, but it does not involve the three-stage series use of hydrogen stream, nor does it involve the suspension bed hydrocracking process or the ebullated bed hydrocracking process, which is different from the method of the present application.

[0010] Chinese patent ZL200910003886.4 A hydrocarbon hydrogenation combined method of coal tar hydrogenation process, the first stream from the first hydrogenation reaction effluent and the second stream from the second hydrogenation reaction effluent are mixed and then cooled by heat exchanger and then enter the common cold high pressure separation section. The invention has the comprehensive advantages of reducing system pressure drop, shortening start-up, shutdown, accident handling time, enhancing operation stability and reducing investment. The method belongs to parallel hydrogen stream combined treatment method, which is different from the method of the invention.

[0011] Chinese patent ZL201010127976.7 A two-stage hydrocarbon hydrogenation method with high pressure partial series connection, the first hydrogenation reaction effluent is separated by the first hot high pressure separation section to obtain the first hot high pressure oil and the first hot high pressure gas, the first hot high pressure gas is separated by the first cold high pressure separation section to obtain the first cold high pressure gas and the first cold high pressure oil, the first hot high pressure oil and the first cold high pressure gas enter the second hydrogenation reaction section, the second hydrogenation reaction effluent is separated by the second cold high pressure separation section to obtain the second cold high pressure gas and the second cold high pressure oil, and at least part of the second cold high pressure gas is recycled back to the first hydrogenation reaction section. The invention has the remarkable effects of reducing total circulating hydrogen amount, simplifying process and reducing investment, and is particularly suitable for anthracene oil two-stage hydrogenation cracking process to produce diesel oil. The method involves 2 times series use of hydrogen, but does not involve 3 times series use of hydrogen stream, nor involves suspended bed hydrogenation process or boiling bed hydrogenation process, which is different from the method of the invention.

[0012] Chinese patent ZL201210022921.9 A low hydrogen content heavy oil hydrogenation lightening method using hydrogen-donor hydrocarbon, hydrogen-donor hydrocarbon stream rich in hydrogen-donor hydrocarbon is used in heavy oil such as coal tar hydrogenation lightening process, has the effect of inhibiting condensation coking speed, improving coal tar heavy oil hydrogenation conversion process liquid product yield, improving product quality, reducing reaction temperature rise, enhancing device operation stability and safety. The hydrogen-donor hydrocarbon stream can be a partially hydrogenated saturated process of a double ring aromatic hydrocarbon and / or a polycyclic aromatic hydrocarbon, or a hydrogenation reaction effluent or an oil product rich in partially saturated aromatic hydrocarbons obtained by separation process. The precursor of hydrogen-donor solvent oil is coal tar distillate with conventional boiling point of 350-450℃, and the hydrogen-donor solvent oil is mainly composed of hydrocarbon components with conventional boiling point of 350-450℃. The coal tar heavy oil hydrogenation lightening method of the present invention is combined with coal tar light distillate oil hydrogenation conversion method to form a new combined process of full distillate coal tar hydrogenation conversion. The method relates to the combination method of coal tar suspension bed hydrocracking process or coal tar boiling bed hydrocracking process and coal tar distillation distillate oil suspension bed hydrocracking process or coal tar distillation distillate oil boiling bed hydrocracking process, the upstream upflow hydrogenation reaction product is separated into upstream hot high pressure gas and upstream hot high pressure oil in the upstream hot high pressure separator, the stream based on the upstream hot high pressure gas enters the downstream upflow hydrogenation reaction process, but does not involve the hydrogen gas stream 3 times in series use method of the downstream hot high pressure gas in series through the subsequent third hydrogenation reaction process of hydrocarbons, and does not involve the method of the upflow hydrogenation reaction hot high pressure oil directly entering the fourth hydrogenation reaction process such as hydrocracking process, which is different from the method of the present invention.

[0013] Chinese patent ZL201310675395.0 A coal tar multi-stage hydroprocessing process, the full distillate of medium and low temperature coal tar is pumped into an electric desalting unit, and the raw oil after electric desalting enters a flash distillation column; the material obtained from the bottom of the column enters a boiling bed reactor for hydroprocessing pretreatment reaction; the liquid fraction obtained by separation of the pretreatment effluent is subjected to hydrofining reaction with hydrogen, and the hydrofining effluent enters a hydrocracking reactor for hydrocracking reaction; naphtha and diesel are obtained by separation of the effluent, and the unconverted oil is recycled back to the hydrofining reactor. The hydrofining reactor and the hydrocracking reactor are directly connected in the method, and the ammonia in the hydrofining reaction product can inhibit the activity of the hydrocracking catalyst in the hydrocracking reactor, which is particularly unfavorable for the condition of producing more naphtha, because the adsorption of ammonia on the catalyst greatly inhibits the adsorption of diesel components, and there is no 3 times in series use scheme of hydrogen stream, which is different from the method of the present invention.

[0014] A low-temperature coal tar processing method, which comprises the following steps: removing solid residues from the low-temperature coal tar, then pre-treating the low-temperature coal tar, and then fractionating the pre-treated low-temperature coal tar to obtain phenol oil, water and heavy oil; subjecting the obtained phenol oil to phenol extraction to obtain refined phenol and dephenolized oil; mixing the obtained heavy oil and the obtained dephenolized oil, and then feeding the mixture into a ebullated-bed reactor to perform hydrogenation reaction to obtain modified heavy oil and by-product gas containing sulfur and ammonia; subjecting the obtained modified heavy oil to hydrofining and hydrocracking to obtain dry gas, liquefied gas, naphtha, diesel product and tail oil product. The naphtha and diesel obtained by the method are clean and stable in performance, and in addition, a plurality of high-value-added products are obtained. After ebullated-bed hydrogenation treatment, the catalyst life of the fixed-bed reactor is prolonged, and the processing problem of heavy components in the coal tar is solved. The modified heavy oil after ebullated-bed hydrogenation is subjected to hydrofining and hydrocracking, thereby improving the properties of the oil product. In the method, the hydrofining reaction product is first fed into a fractionating column before entering the hydrocracking reactor, the hydrofining product is fractionated to obtain naphtha fraction, diesel fraction, dry gas, liquefied gas and tail oil fraction, the naphtha fraction and the diesel fraction are directly discharged from the device, and the tail oil fraction is mixed with unconverted oil produced after hydrocracking to perform hydrocracking reaction, and the hydrocracking product is fractionated to obtain naphtha fraction, diesel fraction, dry gas, liquefied gas, unconverted oil and tail oil, and the tail oil is partially discharged; the liquid flow path between the hydrofining reactor and the hydrocracking reactor is subjected to fractionation system, the hydrocracking feed is removed of ammonia gas, but the pressure is necessarily reduced instead of being directly connected at high pressure, the process is complex and the investment is large; in addition, the method does not involve a three-series use scheme of hydrogen gas stream, which is different from the method of the present application.

[0015] Chinese patent application No. 201410373486.3 A hydrocarbon hydrogenation method with series operation of upflow bed and fixed bed, particularly suitable for deep hydro-conversion process of medium-low temperature coal tar containing moderate amount of metal compound easy to be hydrogenolyzed, the reaction product of upflow pre-hydrogenation reaction zone R11 contains particulate matter, the particulate matter interception bed provided by series connection of fixed bed pre-hydrogenation reaction zone R12 intercepts particulate matter of predetermined particle size, thereby reducing the amount of particulate matter filling the fixed bed catalyst bed of deep hydro-upgrading reaction process R2 processing the reaction product of R12. The upflow pre-hydrogenation reaction zone R11 can be micro-expanded bed, suspended bed, boiling bed, fixed bed, bubbling bed, etc. The porosity or void equivalent diameter of the fixed bed catalyst bed of pre-hydrogenation reaction zone R12 is smaller than that of the fixed bed catalyst bed of deep hydro-upgrading reaction process R2. In the method, the pre-hydrogenation reaction effluent R1P can enter the hot high-pressure separation process 1THPS to be separated into hot high-pressure vapor gas 1THPV and hot high-pressure oil 1THPL; the hot high-pressure vapor gas 1THPV can enter the deep hydro-upgrading reaction process R2; in the method, a hydrocracking reaction process R3 can be provided to convert the hydro-upgrading heavy oil R2PO-DO mainly composed of hydrocarbons with boiling point higher than 350℃ obtained by separating the hydro-upgrading oil R2PO of the deep hydro-upgrading reaction effluent R2P into hydro-upgrading heavy oil R2PO-DO as raw material into hydrocracking reaction effluent R3P. The liquid flow path between the deep hydro-upgrading reactor and the hydrocracking reactor of the method passes through a fractionation system, and the hydrocracking feed is removed from the ammonia gas, but is necessarily depressurized instead of being directly connected at high pressure, which is complex and has large investment; at the same time, there is no 3-time series use scheme of hydrogen gas stream, which is different from the method of the present application.

[0016] Chinese patent ZL201410732099.4 A coal tar hydroprocessing method, the method is that coal tar and hydrogen first carry out hydrogenation reaction in the hydroprocessing reactor boiling bed reaction zone; the reaction product is dehydrated and fractionated to obtain light components and heavy components, part of the heavy components returns to the boiling bed reaction zone or part of the heavy components is discharged; the light components enter the fixed bed reaction zone of the hydroprocessing reactor for reaction, and the reaction product is fractionated to obtain gas, naphtha and diesel; the hydroprocessing reactor is a concentric cylindrical reactor, including an inner layer and an outer layer cylinder, the inner layer cylinder is a boiling bed reaction zone, and the outer layer cylinder is a fixed bed reaction zone, the boiling bed reaction zone and the fixed bed reaction zone are not connected with each other, and are respectively provided with a feed line and a discharge line. The method can effectively alleviate the temperature rise in the boiling bed reaction zone, reduce the amount of quenching oil, and also can save the heating furnace required for the hydrogenation of the light components in the fixed bed reaction zone in the prior art, thereby saving equipment investment. The boiling bed reaction zone and the fixed bed reaction zone of the method are directly connected, there is no gas-liquid separation process, and there is no 3-time series use scheme of hydrogen gas stream, which is different from the method of the present application.

[0017] Chinese patent ZL201510769120.2 A high-temperature coal tar processing method, the method comprises the following contents: high-temperature coal tar is mixed with solvent oil and then enters a demetallization processor, the effluent obtained after reacting with the filler is contacted with fresh water in a water washing tower, the obtained mixture enters a dehydration tower, and the separated high-temperature coal tar after removing the metal and water are obtained, the obtained high-temperature coal tar enters a ebullated bed reactor for hydrogenation reaction, the reaction effluent is subjected to flash dehydration fractionation to obtain light components and heavy components, the light components enter a fixed bed reactor for hydrogenation reaction, and the reaction product is separated to obtain gas, naphtha and diesel; the separated heavy components are all returned to the ebullated bed reactor for recycling treatment, or part of the heavy components are returned to the ebullated bed reactor, and the remaining part is discharged out of the device. The method can remove the metal in the high-temperature coal tar under mild conditions, and slow down the metal deactivation of the catalyst in the hydrogenation reactor and the rise of the bed pressure drop. The ebullated bed reaction zone and the fixed bed reaction zone are not directly connected at high pressure, but there is a gas-liquid separation process, and the three series use schemes of the hydrogen gas stream are not involved, which is different from the method of the application.

[0018] Chinese patent ZL201611052155.5 A coal tar comprehensive utilization method, comprising the following contents: coal tar and a pretreatment agent enter a pretreatment reactor for mixing, uniform mixing and separation of insoluble substances by sedimentation filtration treatment to obtain purified coal tar; the obtained purified coal tar is mixed with hydrogen and then enters an ebullated bed hydrogenation treatment reaction zone for hydrogenation treatment; the reaction product oil obtained from the ebullated bed hydrogenation treatment reaction zone is sequentially subjected to a fixed bed hydrogenation pretreatment reaction zone and a fixed bed hydrogenation treatment reaction zone arranged in series, and the reaction effluent obtained from the fixed bed hydrogenation treatment reaction zone is separated to obtain gas, naphtha, diesel, wax oil and tail oil. The method has a simple process, only needs to make a simple improvement on the existing device, can greatly prolong the operation cycle of the device, and can maximize the utilization efficiency of the catalyst. In the method, the reaction product oil obtained from the ebullated bed hydrogenation treatment reaction zone is sequentially subjected to the fixed bed hydrogenation pretreatment reaction zone and the fixed bed hydrogenation treatment reaction zone arranged in series, and the reaction effluent obtained from the fixed bed hydrogenation treatment reaction zone is separated to obtain gas, naphtha, diesel, wax oil and tail oil; wherein the fixed bed hydrogenation pretreatment reaction zone comprises at least two hydrogenation pretreatment reactors arranged in parallel, when the pressure drop of any one hydrogenation pretreatment reactor in the fixed bed hydrogenation pretreatment reaction zone reaches a predetermined value, the hydrogenation pretreatment reactor with the pressure drop reaching the predetermined value is cut out from the fixed bed hydrogenation pretreatment reaction zone, and the fixed bed hydrogenation pretreatment reaction zone, the hydrogenation pretreatment reactor with the pressure drop reaching the predetermined value and the fixed bed hydrogenation treatment reaction zone are sequentially connected in series, wherein the predetermined value is 50% to 80% of the upper limit of the pressure drop design. The method does not involve the separation of the reaction product and the series use of the separated gas, which is different from the method of the application.

[0019] Chinese patent ZL201811618736.X A coal tar full fraction ebullated bed-fixed bed combined treatment process, the combined treatment process is that the full fraction coal tar raw material and the auxiliary agent enter the pretreatment tank for mixing, after mixing treatment, liquid-solid separation is carried out, the liquid phase material obtained after separation enters the ebullated bed hydrogenation reaction unit for hydrogenation reaction, the reaction effluent enters the separation tank for gas-liquid separation, after separation, the gas phase material and the liquid phase material are obtained, the liquid phase material is divided into first liquid phase material and second liquid phase material two streams, wherein the first liquid phase material is recycled back to the pretreatment tank; the second liquid phase material enters the fixed bed hydrogenation reaction unit for hydrogenation reaction, and the reaction effluent is fractionated to obtain naphtha, diesel and hydrogenated tail oil. The process can realize efficient utilization of coal tar resources and long-period operation. The method is not directly connected between the ebullated bed reaction zone and the fixed bed reaction zone under high pressure, but there is a gas-liquid separation process, that is, the ebullated bed hydrogenation reaction oil from which most of the ammonia gas is removed enters the fixed bed hydrogenation reaction unit, but it does not involve a three-series use scheme of hydrogen gas stream, which is different from the method of the present application.

[0020] In the introduction of the above-mentioned comparative document, the properties of coal tar, the properties of catalyst, the hydrogenation target, the operating conditions, and the product properties involved in the comparative document become part of the background information of the present application.

[0021] The method described in the present application has not been reported.

[0022] Therefore, the first object of the present application is to propose a combined hydroconversion method of heavy hydrocarbons and medium hydrocarbons using hydrogen in three series.

[0023] The second object of the present application is to propose that the separation process of the third liquid S3L and the fourth liquid S4L can be partially or wholly combined.

[0024] The third object of the present application is to propose an optimized operation scheme of the hot high-pressure separation part TS4 of the fourth hydrogenation product R4P, which is separated into a hot high-vapor TS4V rich in naphtha components and a hot high-oil TS4L, and at least part of the hydrocarbon stream based on the hot high-oil TS4L is returned to the fourth hydrogenation reaction process R4 for short-flow selective hydrocracking reaction, so that the amount of the fourth hydrogenation product oil (containing cracking cycle oil) can be reduced, and the load of the fractionation process can be reduced. SUMMARY

[0025] The combined hydroconversion method of heavy hydrocarbons and medium hydrocarbons using hydrogen in three series of the present application comprises the following processes:

[0026] The heavy hydrocarbon RAF is mainly composed of hydrocarbon components with a conventional boiling point higher than 450℃ and contains at least a part of asphaltene components with a conventional boiling point higher than 510℃;

[0027] middle hydrocarbon RBF, mainly composed of conventional liquid hydrocarbon with conventional boiling point lower than 510℃;

[0028] The first hydrogenation reaction product R1P produced by the hydrogen-rich gas through the first hydrogenation reaction process R1 is separated into hot high-pressure gas S1V and hot high-pressure liquid S1L in the first hot high-pressure separation process S1;

[0029] The second hydrogenation reaction product R2P produced by the hydrogen-rich stream based on the hot high-pressure gas S1V through the second hydrogenation reaction process R2 is separated into hot high-pressure gas S2V and hot high-pressure liquid S2L in the second hot high-pressure separation process S2;

[0030] The third hydrogenation reaction product R3P produced by the hydrogen-rich stream based on the hot high-pressure gas S2V through the third hydrogenation reaction process R3 is separated into hydrogen-rich third separation gas S3V and third hydrogenation product oil S3L in the third separation process S3;

[0031] At least part of the third separation gas S3V is recycled to the first hydrogenation reaction process R1 and / or the second hydrogenation reaction process R2 and / or the third hydrogenation reaction process R3;

[0032] The heavy hydrocarbon RAF is subjected to a hydro-lighening reaction in the hydrogenation reaction process RA, and the heavy hydrocarbon hydrogenation reaction product RAP is separated into hot high-pressure gas SAV and hot high-pressure liquid SAL in the hot high-pressure separation process SA; the hydrogenation reaction process RA uses or does not use a hydrogen-donating hydrocarbon stream;

[0033] The middle hydrocarbon RBF is subjected to a hydro-treating reaction in the hydrogenation reaction process RB, and the middle hydrocarbon hydro-treating reaction product RBP is separated into hot high-pressure gas SBV and hot high-pressure liquid SBL in the hot high-pressure separation process SB;

[0034] When the hydrogenation reaction process RA is carried out in the first hydrogenation reaction process R1, the hydrogenation reaction process RB is carried out in the second hydrogenation reaction process R2, at which time the hot high-pressure gas SAV is used as the hot high-pressure gas S1V, the hot high-pressure liquid SAL is used as the hot high-pressure liquid S1L, the hot high-pressure gas SBV is used as the hot high-pressure gas S2V, and the hot high-pressure liquid SBL is used as the hot high-pressure liquid S2L;

[0035] Or when the hydrogenation reaction process RB is carried out in the first hydrogenation reaction process R1, the hydrogenation reaction process RA is carried out in the second hydrogenation reaction process R2, at which time the hot high-pressure gas SBV is used as the hot high-pressure gas S1V, the hot high-pressure liquid SBL is used as the hot high-pressure liquid S1L, the hot high-pressure gas SAV is used as the hot high-pressure gas S2V, and the hot high-pressure liquid SAL is used as the hot high-pressure liquid S2L;

[0036] The stream based on the hot high-pressure liquid SAL is separated into residual oil SAL-H mainly composed of hydrocarbon with conventional boiling point higher than 515℃, distillate oil SAL-M mainly composed of hydrocarbon with conventional boiling point of 50-515℃, and gas after pressure reduction.

[0037] At least a part of the distillate oil SAL-LM enters the hydrogenation reaction process RB and / or the third hydrogenation reaction process R3.

[0038] The present application, generally, based on the separation of the hot high-liquid phase SAL into a residue oil SAL-H mainly composed of hydrocarbons with a conventional boiling point higher than 515℃, a distillate oil SAL-M1 mainly composed of hydrocarbons from carbon 12 to 515℃, a distillate oil SAL-M2 mainly composed of hydrocarbons from carbon 5 to carbon 11, and a gas after the pressure reduction of the stream of the hot high-liquid phase SAL;

[0039] Part of the residue oil SAL-H is recycled to the hydrogenation reaction process RA for reaction;

[0040] At least a part of the distillate oil SAL-M1 enters the hydrogenation reaction process RB;

[0041] At least a part of the distillate oil SAL-M2 enters the third hydrogenation reaction process R3.

[0042] The present application, generally, the thermal processing process of the hydrocarbon oil is selected from a hydrocarbon oil coking process or / and a hydrocarbon oil catalytic cracking process and / or a hydrocarbon oil catalytic pyrolysis process;

[0043] The heavy hydrocarbon RAF is selected from one or more of the following materials:

[0044] ① The heavy oil fraction of low-temperature coal tar and the heavy oil fraction obtained from the thermal processing process thereof;

[0045] ② The heavy oil fraction of medium-temperature coal tar and the heavy oil fraction obtained from the thermal processing process thereof;

[0046] ③ The heavy oil fraction of high-temperature coal tar and the heavy oil fraction obtained from the thermal processing process thereof;

[0047] ④ The heavy oil fraction product of petroleum-based heavy oil and the heavy oil fraction product obtained from the thermal processing process thereof;

[0048] ⑤ The heavy oil fraction product of shale oil-based heavy oil and the heavy oil fraction product obtained from the thermal processing process thereof;

[0049] ⑥ The heavy oil fraction product of oil sand-based heavy oil and the heavy oil fraction product obtained from the thermal processing process thereof;

[0050] The medium hydrocarbon RBF is selected from one or more of the following materials:

[0051] ① The medium distillate oil of low-temperature coal tar and the hydrocarbon oil obtained from the thermal processing process thereof;

[0052] ② The medium distillate oil of medium-temperature coal tar and the hydrocarbon oil obtained from the thermal processing process thereof;

[0053] ③ The medium distillate oil of high-temperature coal tar and the hydrocarbon oil obtained from the thermal processing process thereof;

[0054] ④ The medium distillate oil of petroleum-based heavy oil and the hydrocarbon oil obtained from the thermal processing process thereof;

[0055] ⑤ Middle distillate oil from shale oil and hydrocarbon oils obtained from its thermal processing;

[0056] ⑥ Petroleum sand-based middle distillate oil and hydrocarbon oils obtained from its thermal processing.

[0057] In this invention, the material stream based on the hot high-performance liquid separation process SBL enters the fourth hydrogenation reaction process R4, which includes at least a hydrocracking function, to generate the fourth hydrogenation reaction product R4P. The fourth hydrogenation reaction product R4P is separated to obtain the fourth hydrogen-rich gas V40 and the fourth hydrogenation product oil L40. At least a portion of the fourth hydrogen-rich gas V40 is returned to the fourth hydrogenation reaction process R4 for recycling.

[0058] In this invention, the material from the hot high-pressure liquid separation process (SBL) undergoes a pressure reduction process with the lowest possible pressure before entering the fourth hydrogenation reaction process (R4) at an operating pressure value close to the operating pressure of the hot high-pressure liquid separation process (SBL).

[0059] In this invention, the separation process of the third hydrogenated oil S3L is generally shared with the separation process of the fourth hydrogenated oil L40, either partially or entirely.

[0060] In this invention, typically, the RO-TORA circulating oil used in the hydrotreating process RA is returned to the RA for recycling.

[0061] RO-TORA circulating oil can be selected from one or more of the following:

[0062] ① The separation liquid obtained by separating the intermediate or final product of the hydrogenation reaction process RA;

[0063] ②At least a portion of the hot high-temperature liquid separation solution (SAL) was prepared.

[0064] ③ The hydrocarbon oil obtained by separating the stream based on hot high-efficiency liquid separation (SAL) mainly consists of hydrocarbons with conventional boiling points greater than 515℃;

[0065] ④ The hydrocarbon oil obtained by separating the stream based on hot high-efficiency liquid separation (SAL) mainly consists of hydrocarbons with conventional boiling points greater than 350℃;

[0066] ⑤ The distillate oil obtained by separating the stream based on hot high-efficiency liquid separation (SAL) mainly consists of hydrocarbons with conventional boiling points greater than 220℃;

[0067] ⑥ The separation liquid obtained from the intermediate or final product of the hydrogenation reaction process RB is recycled back to the hydrogenation reaction process RA;

[0068] ⑦ Partial hot high-temperature liquid separation SBL;

[0069] ⑧Separate the hydrocarbon oil obtained from the stream based on hot high-temperature liquid separation (SBL), which is mainly composed of hydrocarbons with conventional boiling points greater than 515℃;

[0070] • separating the intermediate or final product of the fourth hydrogenation reaction process R4 to obtain a hydrocarbon liquid consisting essentially of hydrocarbons having a conventional boiling point greater than 220°C;

[0071] • separating the intermediate or final product of the fourth hydrogenation reaction process R4 to obtain a hydrocarbon liquid consisting essentially of hydrocarbons having a conventional boiling point greater than 350°C;

[0072] • separating the product of the fourth hydrogenation reaction process R4 to obtain a hot high pressure separation liquid;

[0073] • recycling oil RO-TORA is used as a heat carrying oil to carry the heat of reaction or as a hydrogen donor stream containing hydrogen donor hydrocarbons, and the recycling oil RO-TORA or the recycling oil RO-TORA is mixed with the intermediate product of the hydrogenation reaction process RA and the heavy hydrocarbon RAF or the intermediate hydrogenation product of the heavy hydrocarbon RAF.

[0074] • in the hydrogenation reaction process RA, the ratio of the weight flow rate of the recycling oil RO-TORA to the weight flow rate of the heavy hydrocarbon RAF is K100, and K100 is selected from one of the following:

[0075] • 0.01 to 0.20;

[0076] • 0.20 to 0.80;

[0077] • 0.80 to 2.00;

[0078] • 2.00 to 10.00.

[0079] • in the hydrogenation reaction process RB, the recycling oil RO-TORB used is returned to the hydrogenation reaction process RB for recycling;

[0080] • the recycling oil RO-TORB is selected from one or more of the following:

[0081] • separating the intermediate or final product of the hydrogenation reaction process RB to obtain a separation liquid;

[0082] • part of the hot high pressure separation liquid SBL;

[0083] • separating a stream based on the hot high pressure separation liquid SBL to obtain a hydrocarbon oil consisting essentially of hydrocarbons having a conventional boiling point greater than 350°C;

[0084] • separating the fourth hydrogenation reaction product R4P to obtain a distillate oil consisting essentially of hydrocarbons having a conventional boiling point of 220 to 515°C;

[0085] • separating the intermediate or final product of the fourth hydrogenation reaction process R4 to obtain a hydrocarbon oil consisting essentially of hydrocarbons having a conventional boiling point of 220 to 515°C;

[0086] v. separating the intermediate or final product of the fourth hydroprocessing reaction R4 to obtain a hydrocarbon oil mainly consisting of hydrocarbons with a conventional boiling point of 330-515°C;

[0087] vi. separating the product of the fourth hydroprocessing reaction R4 to obtain a separated liquid of the hot high-pressure separation process.

[0088] In the present invention, generally, the ratio of the weight flow rate of the recycle oil RO-TORB used in the hydroprocessing reaction RB to the weight flow rate of the medium hydrocarbon RBF is K200, and K200 can be selected from one of the following:

[0089] i. 0.20-0.80;

[0090] ii. 0.80-2.00;

[0091] iii. 2.00-10.00.

[0092] In the present invention, generally, the recycle oil RO-TOR4 used in the fourth hydroprocessing reaction R4 is returned to the fourth hydroprocessing reaction R4 for recycling;

[0093] The recycle oil RO-TOR4 can be selected from one or more of the following:

[0094] i. separating the intermediate or final product of the fourth hydroprocessing reaction R4 to obtain a hydrocarbon liquid mainly consisting of hydrocarbons with a conventional boiling point of greater than 220°C;

[0095] ii. separating the intermediate or final product of the fourth hydroprocessing reaction R4 to obtain a hydrocarbon liquid mainly consisting of hydrocarbons with a conventional boiling point of greater than 350°C;

[0096] iii. separating the intermediate or final product of the fourth hydroprocessing reaction R4 to obtain a hydrocarbon liquid mainly consisting of hydrocarbons with a conventional boiling point of greater than 350°C;

[0097] iv. separating the product of the fourth hydroprocessing reaction R4 to obtain a separated liquid of the hot high-pressure separation process.

[0098] In the present invention, generally, the ratio of the weight flow rate of the recycle oil RO-TOR4 used in the fourth hydroprocessing reaction R4 to the weight flow rate of the fresh conventional liquid hydrocarbon feed R7F of the fourth hydroprocessing reaction R4 is K700, and K700 can be selected from one of the following:

[0099] i. 0.20-0.80;

[0100] ii. 0.80-2.00.

[0101] In the present invention, generally, the heavy hydrocarbon RAF and the medium hydrocarbon RB are from a distillation process of medium-low temperature coal tar;

[0102] The hydrogenation reaction process RA performs a hydrogenation lightening reaction of the heavy hydrocarbon RAF using a suspension bed hydrogenation reaction mode or a boiling bed hydrogenation reaction mode, with or without a hydrogen-donating solvent; the cracking conversion rate of the hydrocarbon component with a conventional boiling point higher than 515°C in the heavy hydrocarbon RAF is higher than 55% by weight;

[0103] The fractionation bottom oil mainly composed of the hydrocarbon component with a conventional boiling point higher than 515°C obtained by separating the hydrogenation reaction product of the hydrogenation reaction process RA is partially returned to the hydrogenation reaction process RA;

[0104] The hydrogenation reaction process RB performs a hydrotreatment reaction of the medium hydrocarbon RAF using a boiling bed hydrogenation reaction mode and / or a fixed bed hydrogenation reaction mode, at least 50% by weight of a hydrodesulfurization reaction and 50% by weight of a hydrodenitrogenation reaction are completed;

[0105] The hydrogenation reaction process RB includes a boiling bed hydrogenation reaction mode, and the hydrocarbon oil mainly composed of the hydrocarbon component with a conventional boiling point higher than 350°C obtained by separating the hydrogenation reaction product of the hydrogenation reaction process RB is partially returned to the hydrogenation reaction process RB;

[0106] The third hydrogenation reaction process R3 performs a hydrotreatment reaction of the medium hydrocarbon RAF using a fixed bed hydrogenation reaction mode, at least 50% by weight of a hydrodesulfurization reaction and 50% by weight of a hydrodenitrogenation reaction are completed.

[0107] In the present application, generally, the cracking conversion rate of the hydrocarbon component with a conventional boiling point higher than 515°C in the heavy hydrocarbon RAF in the hydrogenation reaction process RA is higher than 85% by weight;

[0108] The hydrogenation reaction process RB at least completes 95% by weight of a hydrodesulfurization reaction and 95% by weight of a hydrodenitrogenation reaction;

[0109] The third hydrogenation reaction process R3 at least completes 95% by weight of a hydrodesulfurization reaction and 95% by weight of a hydrodenitrogenation reaction;

[0110] The fourth hydrogenation reaction process R4 uses a fixed bed hydrogenation reaction mode, and at least 90% by weight of a hydrocracking reaction of the hydrocarbon component with a conventional boiling point higher than 350°C in the reaction raw oil is completed.

[0111] In the present application, generally, the fourth hydrogenation reaction process R4, the flow rate of the hydrocarbon with carbon 6 to carbon 8 in the fourth hydrogenation reaction product is more than 40% by weight of the flow rate of the fresh raw oil of the fourth hydrogenation reaction process R4.

[0112] In the present application, generally, the fourth hydrogenation reaction process R4, the flow rate of the hydrocarbon with carbon 6 to carbon 8 in the fourth hydrogenation reaction product is more than 55% by weight of the flow rate of the fresh raw oil of the fourth hydrogenation reaction process R4.

[0113] The present application, generally, a heavy hydrocarbon with low hydrogen content is a fractionation bottom oil from a fractionation process of a material based on medium-low temperature coal tar, mainly composed of hydrocarbons with a conventional boiling point higher than 450 and containing asphaltene;

[0114] The medium hydrocarbon with low hydrogen content is a distillate oil from a fractionation process of a material based on medium-low temperature coal tar and has a carbon residue content lower than 1% by weight;

[0115] The hydrogenation reaction process RA is a slurry bed hydrocracking reaction process, and the operating conditions are: the temperature is 380-450℃, the pressure is 8.0-25.0MPa, the slurry bed hydrogenation catalyst of the hydrogenation reaction process RA at least contains molybdenum sulfide microcrystals, the proportion of the molybdenum sulfide microcrystals is 0.050%-0.500% by weight of the hydrocarbon oil in the reaction liquid phase, the amount of organic metal in the net generated oil of the hydrogenation reaction process RA is lower than 90% by weight of the amount of organic metal in the fresh raw material hydrocarbon of the hydrogenation reaction process RA, and the carbon residue content in the net generated oil of the hydrogenation reaction process RA is lower than 50% of the carbon residue content in the fresh raw material hydrocarbon of the hydrogenation reaction process RA;

[0116] The operating conditions of the hot high-pressure separation process SA are: the temperature is 200-450℃, the pressure is 8.0-25.0MPa, and the volume concentration of hydrogen in the first separation gas S1V is higher than 65% by volume;

[0117] The hydrogenation reaction process RB uses a boiling bed hydrogenation reactor and simultaneously uses or does not use a fixed bed hydrogenation reactor, and the operating conditions are: the temperature is 230-450℃, the pressure is 8.0-25.0MPa; the boiling bed hydrogenation reactor used by the hydrogenation reaction process RB has an expansion ratio of the boiling bed hydrogenation catalyst bed layer of 1.12-1.55, the amount of organic metal in the net generated oil of the hydrogenation reaction process RB is lower than 10% by weight of the amount of organic metal in the fresh raw material hydrocarbon of the second hydrogenation reaction process R2, the carbon residue content in the net generated oil of the hydrogenation reaction process RB is lower than 30% by weight of the carbon residue content in the fresh raw material hydrocarbon of the hydrogenation reaction process RB, the organic sulfur content in the net generated oil of the hydrogenation reaction process RB is lower than 10% by weight of the organic sulfur content in the fresh raw material hydrocarbon of the hydrogenation reaction process RB, and the organic nitrogen content in the net generated oil of the hydrogenation reaction process RB is lower than 20% by weight of the organic nitrogen content in the fresh raw material hydrocarbon of the hydrogenation reaction process RB;

[0118] The operating conditions of the hot high-pressure separation process SB are: the temperature is 200-450℃, the pressure is 8.0-25.0MPa, and the volume concentration of hydrogen in the second separation gas S2V is higher than 65% by volume;

[0119] The third hydrogenation reaction process R3 is a hydrotreating reaction process, and the operating conditions are: temperature 230-450℃, pressure 8.0-25.0MPa, the organic metal content in the net product oil of the third hydrogenation reaction process R3 is less than 10ppm, the organic nitrogen content in the net product oil of the third hydrogenation reaction process R3 is less than 100ppm, and the organic nitrogen content in the net product oil of the third hydrogenation reaction process R3 is less than 50ppm;

[0120] The volume concentration of hydrogen in the third hydrogen-rich gas is greater than 65%.

[0121] In the present application, the operating conditions of the hydrogenation reaction process RA are: temperature 400-440℃, pressure 10.0-18.0MPa, and the carbon residue content in the net product oil of the hydrogenation reaction process RA is less than 80% of the carbon residue content in the fresh feed hydrocarbon of the hydrogenation reaction process RA;

[0122] The operating conditions of the hot high-pressure separation process SA are: temperature 400-440℃, pressure 10.0-18.0MPa, and the volume concentration of hydrogen in the first separation gas S1V is higher than 75vol%;

[0123] The operating conditions of the hydrogenation reaction process RB are: temperature 230-450℃, pressure 10.0-18.0MPa; the hydrogenation reaction process RB uses a boiling bed hydrogenation reactor, the expansion ratio of the boiling bed hydrogenation catalyst bed is 1.2-1.4, the organic metal content in the net product oil of the hydrogenation reaction process RB is less than 5% of the organic metal content in the fresh feed hydrocarbon of the second hydrogenation reaction process R2, the carbon residue content in the net product oil of the hydrogenation reaction process RB is less than 10% of the carbon residue content in the fresh feed hydrocarbon of the hydrogenation reaction process RB, the organic sulfur content in the net product oil of the hydrogenation reaction process RB is less than 5wt% of the organic sulfur content in the fresh feed hydrocarbon of the hydrogenation reaction process RB, and the organic nitrogen content in the net product oil of the hydrogenation reaction process RB is less than 5wt% of the organic nitrogen content in the fresh feed hydrocarbon of the hydrogenation reaction process RB;

[0124] The operating conditions of the hot high-pressure separation process SB are: temperature 200-450℃, pressure 10.0-18.0MPa, and the volume concentration of hydrogen in the second separation gas S2V is higher than 75vol%;

[0125] The third hydrogenation reaction process R3 is a hydrotreating reaction process, and the operating conditions are: temperature 230-450℃, pressure 8.0-25.0MPa, the organic metal content in the net product oil of the third hydrogenation reaction process R3 is less than 2ppm, the organic sulfur content in the net product oil of the third hydrogenation reaction process R3 is less than 10ppm, and the organic nitrogen content in the net product oil of the third hydrogenation reaction process R3 is less than 2ppm;

[0126] The volume concentration of hydrogen in the third hydrogen-rich gas is greater than 75%.

[0127] Generally, the fourth hydroprocessing reaction R4 is operated in a fixed bed hydroprocessing mode to complete at least 50 wt% of the hydrocracking reaction of the hydrocarbon components having a conventional boiling point greater than 350°C in the reaction feedstock oil;

[0128] The fractionated bottom oil containing the hydrocarbon components having a conventional boiling point higher than 350°C obtained from the fourth hydroprocessing reaction R4 is at least partially returned to the fourth hydroprocessing reaction R4.

[0129] Generally, the fourth hydroprocessing reaction R4 is operated in a fixed bed hydroprocessing mode to complete at least 70 wt% of the hydrocracking reaction of the hydrocarbon components having a conventional boiling point greater than 350°C in the reaction feedstock oil;

[0130] The hydrocarbon oil containing the hydrocarbon components having a conventional boiling point higher than 220°C obtained from the fourth hydroprocessing reaction R4 is at least partially returned to the fourth hydroprocessing reaction R4 to produce more carbon 6 to carbon 8 hydrocarbons.

[0131] Preferably, the fourth hydroprocessing reaction R4 produces a net product oil having an organic metal content of less than 2 ppm, an organic sulfur content of less than 2 ppm, and an organic nitrogen content of less than 10 ppm.

[0132] Generally, the fourth hydroprocessing reaction R4 is operated in a fixed bed hydroprocessing mode to complete the hydrocracking reaction of all the hydrocarbon components having a conventional boiling point greater than 350°C in the reaction feedstock oil;

[0133] The fourth hydroprocessing reaction R4 is operated in a fixed bed hydroprocessing mode to complete more than 80% of the hydrocracking reaction of the hydrocarbon components having a conventional boiling point greater than 280°C in the reaction feedstock oil.

[0134] Generally, the naphtha obtained from the fourth hydroprocessing reaction is separated for catalytic reforming reaction to produce aromatics;

[0135] The hydrogen-rich gas based on the gaseous product from the catalytic reforming reaction is introduced into the first hydroprocessing reaction R1 and / or the second hydroprocessing reaction R2 and / or the third hydroprocessing reaction R3 and / or the fourth hydroprocessing reaction R4.

[0136] Generally, the heavy hydrocarbon is a low hydrogen content heavy hydrocarbon having a hydrogen content of less than 9 wt% of the hydrocarbons having a conventional boiling point higher than 450°C;

[0137] The medium hydrocarbon is a low hydrogen content medium hydrocarbon having a hydrogen content of less than 10.5 wt% of the hydrocarbons having a conventional boiling point lower than 515°C.

[0138] Generally, the heavy hydrocarbon is a low hydrogen content heavy hydrocarbon, wherein the hydrogen content of the hydrocarbon having a conventional boiling point higher than 450℃ is less than 7.5% by weight;

[0139] The medium hydrocarbon is a low hydrogen content medium hydrocarbon, wherein the hydrogen content of the hydrocarbon having a conventional boiling point lower than 515℃ is less than 9.0% by weight.

[0140] The low hydrogen content heavy hydrocarbon, the low hydrogen content medium hydrocarbon of the present invention can come from a fractionation process of the initial coal tar;

[0141] In the fractionation process of the initial coal tar, the initial coal tar is fractionated into several narrow fraction oils with different boiling ranges, the fraction oil mainly composed of hydrocarbons having a conventional boiling point higher than 450℃ and containing asphaltene as a low hydrogen content heavy hydrocarbon, the distillate oil mainly composed of hydrocarbons having a conventional boiling point lower than 450℃ as a low hydrogen content medium hydrocarbon; with or without the distillate oil mainly composed of hydrocarbons having a carbon number of 5 to 11 going to the third hydrogenation reaction process R3.

[0142] The low hydrogen content heavy hydrocarbon, the low hydrogen content medium hydrocarbon of the present invention can come from a fractionation process of the initial medium-low temperature coal tar, the fractionation process of the initial coal tar simultaneously obtaining a narrow fraction distillate oil rich in phenols as a phenol oil for use;

[0143] The dephenolized oil obtained after the phenol oil is dephenolized goes to the second hydrogenation reaction process R2 or the third hydrogenation reaction process R3.

[0144] Generally, the low hydrogen content heavy hydrocarbon, the low hydrogen content medium hydrocarbon of the present invention can come from a fractionation process of the initial medium-low temperature coal tar;

[0145] Before the initial medium-low temperature coal tar goes to the fractionation process of the initial medium-low temperature coal tar, one or more of the following processes are completed:

[0146] ① a dehydration process;

[0147] ② a mechanical impurity removal process;

[0148] ③ a coke powder removal process;

[0149] ④ a desalination process to remove at least a part of organic metal;

[0150] ⑤ an extractive separation process to remove at least a part of asphaltene.

[0151] The fourth hydrogenation reaction product R4P of the present invention can be separated into a hot high-pressure gas TS4V and a hot high-pressure liquid TS4L in a hot high-pressure separation process TS4;

[0152] Based on the hot high-pressure gas TS4V, a cold high-pressure gas CS4V and a cold high-pressure liquid CS4L are separated in a cold high-pressure separation process CS4;

[0153] The separation and fractionation process of the third hydrogenation product S3L is partially or wholly combined with the separation and fractionation process of the cold high pressure separation CS4L;

[0154] The separation and fractionation process of the hot high pressure separation TS4L is not combined with the separation and fractionation process of the third hydrogenation product S3L and the cold high pressure separation CS4L.

[0155] Generally, the present application uses a boiling bed hydrogenation reactor in the hydrogenation reaction process RB and uses a fixed bed hydrogenation reactor upstream and / or downstream of the boiling bed hydrogenation reactor.

[0156] Generally, the present application uses a hydrogenation cracking catalyst and a hydrogenation refining catalyst in the fourth hydrogenation reaction process R4, and the hydrogenation refining catalyst bed is upstream and / or downstream of the hydrogenation cracking catalyst bed.

[0157] Generally, the present application uses one or two or more catalysts in series in the second hydrogenation reaction process R2.

[0158] Generally, the fourth hydrogenation product R4P can be separated into a hot high pressure separation gas TS4V rich in carbon 6 to carbon 8 components and a hot high pressure separation oil TS4L in the fourth hot high pressure separation process TS4 with or without stripping hydrogen.

[0159] At least part of the hydrocarbon stream based on the hot high pressure separation oil TS4L is recycled to the fourth hydrogenation reaction process R4 for hydrogenation cracking reaction.

[0160] Generally, the present application uses the following path for the part of the high pressure recycle oil TS4LR to be recycled to the fourth hydrogenation reaction process R4 for hydrogenation cracking reaction:

[0161] The recycle oil is cooled by the heat exchanger HX and then returned to the inlet of the catalyst bed in the rear part of the fourth hydrogenation reaction process R4 to serve as a cooling medium to reduce the amount of quenching recycle hydrogen.

[0162] The heat exchanger HX can be used to preheat the hydrocarbon material in the fractionation process of the fourth hydrogenation product. DETAILED DESCRIPTION

[0163] The present application is described in detail below.

[0164] The pressure mentioned in the present application refers to absolute pressure.

[0165] The conventional boiling point mentioned in the present application refers to the vapor-liquid equilibrium temperature of a substance at one atmosphere of pressure.

[0166] The conventional boiling range mentioned in the present application refers to the conventional boiling point range of a fraction.

[0167] Unless otherwise specified, the specific gravity mentioned in this invention refers to the ratio of the density of the liquid at normal pressure and 15.6°C to the density of water at normal pressure and 15.6°C.

[0168] Unless otherwise specified, the composition, concentration, content, or yield of the components described in this invention are all weight-based values.

[0169] The conventional gaseous hydrocarbons mentioned in this invention refer to hydrocarbons that are in a gaseous state under normal conditions, including methane, ethane, propane, and butane.

[0170] The conventional liquid hydrocarbons described in this invention refer to hydrocarbons that are liquid under normal conditions, including pentane and hydrocarbons with higher boiling points.

[0171] The impurity elements mentioned in this invention refer to non-hydrogen, non-carbon, and non-metallic components in the raw oil, such as oxygen, sulfur, nitrogen, and chlorine.

[0172] The impurity components mentioned in this invention refer to the hydrogenation conversion products of non-hydrocarbon components in the feedstock oil, such as water, ammonia, hydrogen sulfide, and hydrogen chloride.

[0173] The naphtha component mentioned in this invention refers to a conventional liquid hydrocarbon with a boiling point below 180°C.

[0174] The diesel fuel components described in this invention refer to hydrocarbons with a conventional boiling point of 180–350°C.

[0175] The wax oil component described in this invention refers to hydrocarbons with a conventional boiling point of 350–530°C.

[0176] The residue oil component described in this invention refers to hydrocarbons with a conventional boiling point above 515°C and containing asphaltenes with a conventional boiling point above 530°C.

[0177] The hydrogen-oil volume ratio mentioned in this invention refers to the ratio of the standard state volumetric flow rate of hydrogen to the volumetric flow rate of a specified oil stream at atmospheric pressure and 20°C.

[0178] The gravimetric chemical hydrogen consumption of the hydrogenation reaction process of heavy oil R10F described in this invention refers to the weight of hydrogen consumed per unit weight of heavy oil R10F for the chemical reaction, for example, 2.00%.

[0179] The heavy oil suspension bed hydrogenation reaction process described in this invention has no restrictions on the gas-liquid contact method within the suspension bed hydrogenation reactor; it can be any effective method.

[0180] The heavy oil suspension bed hydrogenation reaction process described in this invention uses a particulate heavy oil suspension bed hydrogenation catalyst that is suspended in the liquid phase of the reaction process to form an oil slurry in which catalyst particles are dispersed. Therefore, it can also be called a heavy oil slurry bed hydrogenation reaction process.

[0181] The heavy oil suspended bed hydrogenation reaction process of the present application is generally an upflow hydrogenation reactor, and the main direction of macro flow of the process medium in the reaction space or hydrogenation catalyst bed is from bottom to top.

[0182] The upflow expanded bed reactor of the present application belongs to an upflow expanded bed reactor.

[0183] The upflow expanded bed reactor of the present application is a vertical upflow reactor, and belongs to an expanded bed catalytic reactor when catalyst is used. Vertical means that the central axis of the reactor in working state is perpendicular to the ground. Upflow means that the main flow direction of the material is from bottom to top through the reaction space or catalyst bed or co-current flow with the upward catalyst. Expanded bed means that the catalyst bed in working state is in an expanded state, and the expanded bed ratio of the catalyst bed is defined as the ratio KBED of the maximum height CWH of the catalyst bed in working state when the reaction raw material passes through to the height CUH of the catalyst bed in empty bed static state. Generally, KBED is lower than 1.10, which is called micro-expanded bed, KBED is between 1.25 and 1.55, which is called boiling bed, and the suspended bed is considered as the most extreme form of expanded bed.

[0184] The back-mixed flow expanded bed reaction zone of the present application refers to the operation mode of the reaction zone of the expanded bed reactor, which has liquid back-mixing or circulating liquid. Back-mixed flow or circulating liquid refers to at least part of the liquid phase XK-L of the intermediate product XK or the final product XK at the process point K returning to the upstream reaction zone of the stream XK as a circulating liquid stream XK-LR, and the reaction product of the circulating liquid stream XK-LR flows through the K point and exists in XK. The back-mixed flow forming mode can be any suitable mode, such as setting an internal inner loop cylinder, an internal outer loop cylinder, an internal liquid collecting cup + flow guide pipe + circulating pump, an external circulating pipe, etc.

[0185] The liquid collecting cup or liquid collector arranged in the reactor of the present application refers to a container arranged in the reactor for collecting liquid, which is usually open at the top or top side and has a flow guide pipe installed at the bottom or bottom side for discharging the collected liquid. The top liquid collector of the expanded bed reactor is usually installed in the liquid removal zone of the gas-liquid material to obtain a liquid and gas-liquid mixed phase stream or a liquid and gas.

[0186] The suspended bed reactor of the present application can be in any suitable form, which can be an empty cylinder suspended bed reactor to form plug flow or back-mixed flow with internal circulation, can be an internal circulation flow guide cylinder to form internal inner loop flow or internal outer loop flow, can be an external circulation pipe to make the liquid in the upper reaction space flow into the lower reaction space to form an external circulation flow type of back-mixed flow, or can be a top product liquid collection and flow guide system to form a forced internal circulation flow type of back-mixed flow through a circulating pressurization system.

[0187] The hot high-gravity separator according to the present application refers to a gas-liquid separation device for separating intermediate or final products of hydrogenation reaction.

[0188] The suspended bed hydrogenation reactor according to the present application can operate in the following modes:

[0189] ① The suspended bed hydrogenation reactor;

[0190] ② The hydrogenation reactor with a combined bed of suspended bed and boiling bed, which can unload the boiling bed catalyst with reduced activity from the bottom of the bed in a batch mode, and can supplement fresh boiling bed catalyst from the upper part of the bed in a batch mode to maintain the amount of boiling bed catalyst in the bed.

[0191] The boiling bed hydrogenation reactor according to the present application can operate in the following modes: no catalyst replacement during operation, or unloading the boiling bed catalyst with reduced activity from the bottom of the bed in a batch mode, and supplementing fresh boiling bed catalyst from the upper part of the bed in a batch mode to maintain the amount of boiling bed catalyst in the bed, or other catalyst loading and unloading modes.

[0192] The following describes the characteristic part of the present application.

[0193] The combined hydrogenation conversion method of heavy hydrocarbon and medium hydrocarbon using hydrogen in three stages in series according to the present application comprises the following processes:

[0194] The heavy hydrocarbon RAF mainly consists of hydrocarbon components with a conventional boiling point higher than 450℃ and contains at least a part of asphaltene components with a conventional boiling point higher than 510℃;

[0195] The medium hydrocarbon RBF mainly consists of conventional liquid hydrocarbon components with a conventional boiling point lower than 510℃;

[0196] The hydrogen-rich gas is subjected to a first hydrogenation reaction process R1 to produce a first hydrogenation reaction product R1P, which is separated into a hot high-gravity gas S1V and a hot high-gravity liquid S1L in a first hot high-pressure separation process S1;

[0197] The hydrogen-rich stream based on the hot high-gravity gas S1V is subjected to a second hydrogenation reaction process R2 to produce a second hydrogenation reaction product R2P, which is separated into a hot high-gravity gas S2V and a hot high-gravity liquid S2L in a second hot high-pressure separation process S2;

[0198] The hydrogen-rich stream based on the hot high-gravity gas S2V is subjected to a third hydrogenation reaction process R3 to produce a third hydrogenation reaction product R3P, which is separated into a hydrogen-rich third separation gas S3V and a third hydrogenation product oil S3L in a third separation process S3;

[0199] At least a part of the third separation gas S3V is recycled to the first hydrogenation reaction process R1 and / or the second hydrogenation reaction process R2 and / or the third hydrogenation reaction process R3.

[0200] The heavy hydrocarbon RAF is subjected to a hydro-lightrning reaction in a hydro-reaction process RA, and a heavy hydro-reaction product RAP is separated into a hot high-gas SAV and a hot high-liquid SAL in a hot high-pressure separation process SA;

[0201] The medium hydrocarbon RBF is subjected to a hydro-treatment reaction in a hydro-reaction process RB, and a medium hydro-treatment product RBP is separated into a hot high-gas SBV and a hot high-liquid SBL in a hot high-pressure separation process SB;

[0202] When the hydro-reaction process RA is carried out in a first hydro-reaction process R1, the hydro-reaction process RB is carried out in a second hydro-reaction process R2, at this time, the hot high-gas SAV is the hot high-gas S1V and the hot high-liquid SAL is the hot high-liquid S1L, and the hot high-gas SBV is the hot high-gas S2V and the hot high-liquid SBL is the hot high-liquid S2L;

[0203] Or when the hydro-reaction process RB is carried out in a first hydro-reaction process R1, the hydro-reaction process RA is carried out in a second hydro-reaction process R2, at this time, the hot high-gas SBV is the hot high-gas S1V and the hot high-liquid SBL is the hot high-liquid S1L, and the hot high-gas SAV is the hot high-gas S2V and the hot high-liquid SAL is the hot high-liquid S2L;

[0204] The hot high-liquid SAL is separated into a residue oil SAL-H mainly composed of hydrocarbons with a conventional boiling point higher than 515℃, a distillate oil SAL-M1 mainly composed of hydrocarbons with a conventional boiling point from carbon 12 to 515℃, a distillate oil SAL-M2 mainly composed of hydrocarbons with a conventional boiling point from carbon 5 to carbon 11, and a gas after being depressurized;

[0205] At least a part of the distillate oil SAL-LM enters the hydro-reaction process RB and / or a third hydro-reaction process R3.

[0206] In the present application, generally, the hot high-liquid SAL is separated into a residue oil SAL-H mainly composed of hydrocarbons with a conventional boiling point higher than 515℃, a distillate oil SAL-M1 mainly composed of hydrocarbons with a conventional boiling point from carbon 12 to 515℃, a distillate oil SAL-M2 mainly composed of hydrocarbons with a conventional boiling point from carbon 5 to carbon 11, and a gas after being depressurized;

[0207] Part of the residue oil SAL-H is recycled to the hydro-reaction process RA;

[0208] At least a part of the distillate oil SAL-M1 enters the hydro-reaction process RB;

[0209] At least a part of the distillate oil SAL-M2 enters the third hydro-reaction process R3.

[0210] Generally, the hydrocarbon oil thermal processing process is selected from the group consisting of hydrocarbon oil coking process and / or hydrocarbon oil catalytic cracking process and / or hydrocarbon oil catalytic pyrolysis process.

[0211] The heavy hydrocarbon RAF is selected from one or more of the following:

[0212] ① Low temperature coal tar heavy oil fraction and heavy oil fraction obtained from thermal processing of the heavy oil fraction;

[0213] ② Medium temperature coal tar heavy oil fraction and heavy oil fraction obtained from thermal processing of the heavy oil fraction;

[0214] ③ High temperature coal tar heavy oil fraction and heavy oil fraction obtained from thermal processing of the heavy oil fraction;

[0215] ④ Petroleum-based heavy oil and heavy oil fraction product obtained from thermal processing of the heavy oil;

[0216] ⑤ Shale oil-based heavy oil and heavy oil fraction product obtained from thermal processing of the heavy oil;

[0217] ⑥ Oil sand-based heavy oil and heavy oil fraction product obtained from thermal processing of the heavy oil;

[0218] The medium hydrocarbon RBF is selected from one or more of the following:

[0219] ① Low temperature coal tar heavy oil fraction and heavy oil fraction obtained from thermal processing of the heavy oil fraction;

[0220] ② Medium temperature coal tar heavy oil fraction and heavy oil fraction obtained from thermal processing of the heavy oil fraction;

[0221] ③ High temperature coal tar heavy oil fraction and heavy oil fraction obtained from thermal processing of the heavy oil fraction;

[0222] ④ Petroleum-based heavy oil and heavy oil fraction product obtained from thermal processing of the heavy oil;

[0223] ⑤ Shale oil-based heavy oil and heavy oil fraction product obtained from thermal processing of the heavy oil;

[0224] ⑥ Oil sand-based heavy oil and heavy oil fraction product obtained from thermal processing of the heavy oil.

[0225] Generally, the hot high-boiling liquid SBL-based stream enters a fourth hydrogenation reaction process R4 containing at least a hydrocracking function to generate a fourth hydrogenation reaction product R4P, and the fourth hydrogenation reaction product R4P is separated to obtain a fourth hydrogen-rich gas V40 and a fourth hydrogenation product oil L40, and at least part of the fourth hydrogen-rich gas V40 is recycled to the fourth hydrogenation reaction process R4.

[0226] Generally, the hot high-boiling liquid SBL-based stream, after passing through a pressure reduction process as low as possible, enters the fourth hydrogenation reaction process R4 at an operating pressure close to the operating pressure of the hot high-boiling liquid SBL.

[0227] Generally, the present invention, the separation process of the third hydrogenation product oil S3L, and the separation process of the fourth hydrogenation product oil L40, are partially or totally shared.

[0228] Generally, the present invention, the hydrogenation reaction process RA, uses the recycle oil RO-TORA to return to the hydrogenation reaction process RA for recycling reaction.

[0229] The recycle oil RO-TORA can be selected from one or more of the following:

[0230] ① The separation liquid obtained by separating the intermediate product or the final product of the hydrogenation reaction process RA;

[0231] ② At least a part of the hot high-pressure separation liquid SAL;

[0232] ③ The hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point greater than 515℃ obtained by separating the stream based on the hot high-pressure separation liquid SAL;

[0233] ④ The hydrocarbon liquid mainly composed of hydrocarbons with a conventional boiling point greater than 350℃ obtained by separating the stream based on the hot high-pressure separation liquid SAL;

[0234] ⑤ The distillate oil mainly composed of hydrocarbons with a conventional boiling point greater than 220℃ obtained by separating the stream based on the hot high-pressure separation liquid SAL;

[0235] ⑥ The separation liquid obtained by separating the intermediate product or the final product of the hydrogenation reaction process RB, which is recycled back to the hydrogenation reaction process RA;

[0236] ⑦ A part of the hot high-pressure separation liquid SBL;

[0237] ⑧ The hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point greater than 515℃ obtained by separating the stream based on the hot high-pressure separation liquid SBL;

[0238] ⑨ The hydrocarbon liquid mainly composed of hydrocarbons with a conventional boiling point greater than 220℃ obtained by separating the intermediate product or the final product of the fourth hydrogenation reaction process R4;

[0239] ⑩ The hydrocarbon liquid mainly composed of hydrocarbons with a conventional boiling point greater than 350℃ obtained by separating the intermediate product or the final product of the fourth hydrogenation reaction process R4;

[0240] The separation liquid of the hot high-pressure separation process obtained by separating the product of the fourth hydrogenation reaction process R4;

[0241] The recycle oil RO-TORA is used as a heat-carrying oil carrying reaction heat or a hydrogen-containing hydrocarbon stream containing hydrogen-containing hydrocarbons, and the recycle oil RO-TORA or the recycle oil RO-TORA is mixed with the heavy hydrocarbon RAF or the intermediate hydrogenation product of the heavy hydrocarbon RAF in the intermediate product of the hydrogenation reaction process RA.

[0242] Generally, in the hydrogenation reaction process RA, the ratio of the weight flow rate of the recycle oil RO-TORA to the weight flow rate of the heavy hydrocarbon RAF is K100, and K100 can be selected from one of the following:

[0243] ① 0.01-0.20;

[0244] ② 0.20-0.80;

[0245] ③ 0.80-2.00;

[0246] ④ 2.00-10.00.

[0247] Generally, in the hydrogenation reaction process RB, the recycle oil RO-TORB used is returned to the hydrogenation reaction process RB for recycling;

[0248] The recycle oil RO-TORB can be selected from one or more of the following:

[0249] ① a separation liquid obtained by separating an intermediate product or a final product of the hydrogenation reaction process RB;

[0250] ② a part of the hot high-pressure separation liquid SBL;

[0251] ③ a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point greater than 350°C, obtained by separating a stream based on the hot high-pressure separation liquid SBL;

[0252] ④ a distillate oil mainly composed of hydrocarbons with a conventional boiling point of 220-515°C, obtained by separating a fourth hydrogenation reaction product R4P;

[0253] ④ a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point of 220-515°C, obtained by separating an intermediate product or a final product of the fourth hydrogenation reaction process R4;

[0254] ⑤ a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point of 330-515°C, obtained by separating an intermediate product or a final product of the fourth hydrogenation reaction process R4;

[0255] ⑥ a separation liquid of a hot high-pressure separation process obtained by separating a product of the fourth hydrogenation reaction process R4.

[0256] Generally, in the hydrogenation reaction process RB, the ratio of the weight flow rate of the recycle oil RO-TORB used to the weight flow rate of the medium hydrocarbon RBF is K200, and K200 can be selected from one of the following:

[0257] ① 0.20-0.80;

[0258] ② 0.80-2.00;

[0259] ③ 2.00-10.00.

[0260] Generally, the present application, in the fourth hydroreaction process R4, uses the recycle oil RO-TOR4 to return to the fourth hydroreaction process R4 for recycling reaction;

[0261] The recycle oil RO-TOR4 can be selected from one or more of the following:

[0262] ① The hydrocarbon liquid mainly composed of hydrocarbons with conventional boiling point greater than 220℃ obtained by separating the intermediate product or the final product of the fourth hydroreaction process R4;

[0263] ② The hydrocarbon liquid mainly composed of hydrocarbons with conventional boiling point greater than 350℃ obtained by separating the intermediate product or the final product of the fourth hydroreaction process R4;

[0264] ③ The hydrocarbon liquid mainly composed of hydrocarbons with conventional boiling point greater than 350℃ obtained by separating the intermediate product or the final product of the fourth hydroreaction process R4;

[0265] ④ The separation liquid of the hot high-pressure separation process obtained by separating the product of the fourth hydroreaction process R4.

[0266] Generally, in the fourth hydroreaction process R4, the ratio of the weight flow rate of the recycle oil RO-TOR4 to the weight flow rate of the fresh conventional liquid hydrocarbon feed R7F of the fourth hydroreaction process R4 is K700, and K700 can be selected from one of the following:

[0267] ① 0.20-0.80;

[0268] ② 0.80-2.00.

[0269] Generally, in the present application, the heavy hydrocarbon RAF and the medium hydrocarbon RB are obtained from the distillation process of the low-temperature coal tar;

[0270] The hydroreaction process RA performs the hydro-lightening reaction of the heavy hydrocarbon RAF, adopts the suspension bed hydroreaction mode or the boiling bed hydroreaction mode, and uses or does not use the hydrogen-donating solvent; the cracking conversion rate of the hydrocarbon component with conventional boiling point greater than 515℃ in the heavy hydrocarbon RAF is higher than 55wt%;

[0271] The fractionation bottom oil mainly composed of the hydrocarbon component with conventional boiling point higher than 515℃ obtained by separating the generated oil of the hydroreaction process RA is partially returned to the hydroreaction process RA;

[0272] The hydroreaction process RB performs the hydrotreating reaction of the medium hydrocarbon RAF, adopts the boiling bed hydroreaction mode and / or the fixed bed hydroreaction mode, and at least completes 50wt% of the hydrodesulfurization reaction and 50wt% of the hydrodenitrogenation reaction;

[0273] The hydrogenation reaction process RB includes a boiling bed hydrogenation reaction mode, and a hydrocarbon oil mainly composed of hydrocarbon components with a conventional boiling point higher than 350°C is obtained by separating the oil generated by the hydrogenation reaction process RB, and is partially returned to the hydrogenation reaction process RB;

[0274] The third hydrogenation reaction process R3 performs a hydroprocessing reaction of the medium weight hydrocarbon RAF, and a fixed bed hydrogenation reaction mode, and at least 50% by weight of a hydrodesulfurization reaction and 50% by weight of a hydrodenitrogenation reaction are completed.

[0275] In the present application, generally, the hydrogenation reaction process RA has a cracking conversion rate of hydrocarbon components with a conventional boiling point higher than 515°C in the heavy hydrocarbon RAF higher than 85% by weight;

[0276] The hydrogenation reaction process RB has at least 95% by weight of a hydrodesulfurization reaction and 95% by weight of a hydrodenitrogenation reaction completed.

[0277] The third hydrogenation reaction process R3 has at least 95% by weight of a hydrodesulfurization reaction and 95% by weight of a hydrodenitrogenation reaction completed.

[0278] The fourth hydrogenation reaction process R4 has a fixed bed hydrogenation reaction mode, and at least 90% by weight of a hydrocracking reaction of hydrocarbon components with a conventional boiling point higher than 350°C in the reaction raw oil is completed.

[0279] In the present application, generally, the fourth hydrogenation reaction process R4 has a flow rate of hydrocarbons with carbon 6 to carbon 8 in the fourth hydrogenation reaction oil higher than 40% by weight of a flow rate of fresh raw oil of the fourth hydrogenation reaction process R4.

[0280] In the present application, generally, the fourth hydrogenation reaction process R4 has a flow rate of hydrocarbons with carbon 6 to carbon 8 in the fourth hydrogenation reaction oil higher than 55% by weight of a flow rate of fresh raw oil of the fourth hydrogenation reaction process R4.

[0281] In the present application, generally, the heavy hydrocarbon with a low hydrogen content is a fractionation bottom oil from a fractionation process based on a material of medium and low temperature coal tar, and is mainly composed of hydrocarbons with a conventional boiling point higher than 450°C and contains asphaltene;

[0282] The medium weight hydrocarbon with a low hydrogen content is a distillate oil from a fractionation process based on a material of medium and low temperature coal tar and has a carbon residue content lower than 1% by weight;

[0283] The hydrogenation reaction process RA is a slurry bed hydrogenation cracking reaction process, and the operating conditions are: a temperature of 380-450°C, a pressure of 8.0-25.0 MPa, and the slurry bed hydrogenation catalyst of the hydrogenation reaction process RA at least contains molybdenum sulfide microcrystals, the proportion of the molybdenum sulfide microcrystals is 0.050%-0.500% by weight of the hydrocarbon oil in the reaction liquid phase, the amount of organic metal in the net generated oil of the hydrogenation reaction process RA is less than 90% by weight of the amount of organic metal in the fresh raw hydrocarbon of the hydrogenation reaction process RA, and the amount of residual carbon in the net generated oil of the hydrogenation reaction process RA is less than 50% of the amount of residual carbon in the fresh raw hydrocarbon of the hydrogenation reaction process RA;

[0284] The operating conditions of the hot high-pressure separation process SA are: a temperature of 200-450°C, a pressure of 8.0-25.0 MPa, and the volume concentration of hydrogen in the first separation gas S1V is higher than 65% by volume;

[0285] The hydrogenation reaction process RB uses a boiling bed hydrogenation reactor with or without a fixed bed hydrogenation reactor, and the operating conditions are: a temperature of 230-450°C, a pressure of 8.0-25.0 MPa; the boiling bed hydrogenation reactor of the hydrogenation reaction process RB has an expansion ratio of 1.12-1.55 for the boiling bed hydrogenation catalyst bed, the amount of organic metal in the net generated oil of the hydrogenation reaction process RB is less than 10% by weight of the amount of organic metal in the fresh raw hydrocarbon of the second hydrogenation reaction process R2, the amount of residual carbon in the net generated oil of the hydrogenation reaction process RB is less than 30% by weight of the amount of residual carbon in the fresh raw hydrocarbon of the hydrogenation reaction process RB, the amount of organic sulfur in the net generated oil of the hydrogenation reaction process RB is less than 10% by weight of the amount of organic sulfur in the fresh raw hydrocarbon of the hydrogenation reaction process RB, and the amount of organic nitrogen in the net generated oil of the hydrogenation reaction process RB is less than 20% by weight of the amount of organic nitrogen in the fresh raw hydrocarbon of the hydrogenation reaction process RB;

[0286] The operating conditions of the hot high-pressure separation process SB are: a temperature of 200-450°C, a pressure of 8.0-25.0 MPa, and the volume concentration of hydrogen in the second separation gas S2V is higher than 65% by volume;

[0287] The third hydrogenation reaction process R3 is a hydrogenation treatment reaction process, and the operating conditions are: a temperature of 230-450°C, a pressure of 8.0-25.0 MPa, the amount of organic metal in the net generated oil of the third hydrogenation reaction process R3 is less than 10 ppm, the amount of organic nitrogen in the net generated oil of the third hydrogenation reaction process R3 is less than 100 ppm, and the amount of organic nitrogen in the net generated oil of the third hydrogenation reaction process R3 is less than 50 ppm;

[0288] The volume concentration of hydrogen in the third hydrogen-rich gas is greater than 65%.

[0289] The present application, generally, the operating conditions of the hydrogenation reaction process RA are: the temperature is 400-440℃, the pressure is 10.0-18.0MPa, the carbon residue content in the net product oil of the hydrogenation reaction process RA is less than 80% of the carbon residue content in the fresh raw hydrocarbon of the hydrogenation reaction process RA;

[0290] The operating conditions of the hot high-pressure separation process SA are: the temperature is 400-440℃, the pressure is 10.0-18.0MPa, the volume concentration of hydrogen in the first separation gas S1V is higher than 75% by volume;

[0291] The operating conditions of the hydrogenation reaction process RB are: the temperature is 230-450℃, the pressure is 10.0-18.0MPa; the boiling bed hydrogenation reactor used by the hydrogenation reaction process RB, the expansion ratio of the boiling bed hydrogenation catalyst bed is 1.2-1.4, the organic metal content in the net product oil of the hydrogenation reaction process RB is less than 5% of the organic metal content in the fresh raw hydrocarbon of the second hydrogenation reaction process R2, the carbon residue content in the net product oil of the hydrogenation reaction process RB is less than 10% of the carbon residue content in the fresh raw hydrocarbon of the hydrogenation reaction process RB, the organic sulfur content in the net product oil of the hydrogenation reaction process RB is less than 5% by weight of the organic sulfur content in the fresh raw hydrocarbon of the hydrogenation reaction process RB, the organic nitrogen content in the net product oil of the hydrogenation reaction process RB is less than 5% by weight of the organic nitrogen content in the fresh raw hydrocarbon of the hydrogenation reaction process RB;

[0292] The operating conditions of the hot high-pressure separation process SB are: the temperature is 200-450℃, the pressure is 10.0-18.0MPa, the volume concentration of hydrogen in the second separation gas S2V is higher than 75% by volume;

[0293] The third hydrogenation reaction process R3 is a hydrogenation treatment reaction process, the operating conditions are: the temperature is 230-450℃, the pressure is 8.0-25.0MPa, the organic metal content in the net product oil of the third hydrogenation reaction process R3 is less than 2ppm, the organic sulfur content in the net product oil of the third hydrogenation reaction process R3 is less than 10ppm, the organic nitrogen content in the net product oil of the third hydrogenation reaction process R3 is less than 2ppm;

[0294] The volume concentration of hydrogen in the third hydrogen-rich gas is greater than 75%.

[0295] The present application, generally, the fourth hydrogenation reaction process R4 adopts a fixed bed hydrogenation reaction mode, and at least 50% by weight of the hydrocarbon components with a conventional boiling point greater than 350℃ in the reaction raw oil is subjected to a hydrocracking reaction;

[0296] The fractionation bottom oil containing the hydrocarbon components with a conventional boiling point higher than 350℃ obtained by separating the product oil of the fourth hydrogenation reaction process R4 is at least partially returned to the fourth hydrogenation reaction process R4.

[0297] Generally, the fourth hydroprocessing reaction process R4 employs a fixed bed hydroprocessing mode to complete hydrocracking reaction of at least 70 wt% of the hydrocarbon components having a conventional boiling point greater than 350°C in the reaction feedstock oil;

[0298] The hydrocarbon oil containing hydrocarbon components having a conventional boiling point higher than 220°C obtained from separation of the fourth hydroprocessing reaction process R4 generated oil is at least partially returned to the fourth hydroprocessing reaction process R4 to produce more carbon 6 to carbon 8 hydrocarbons.

[0299] Preferably, the fourth hydroprocessing reaction process R4 produces a net generated oil having an organic metal content of less than 2 ppm, an organic sulfur content of less than 2 ppm, and an organic nitrogen content of less than 10 ppm.

[0300] In particular, the fourth hydroprocessing reaction process R4 employs a fixed bed hydroprocessing mode to complete hydrocracking reaction of all the hydrocarbon components having a conventional boiling point greater than 350°C in the reaction feedstock oil;

[0301] The fourth hydroprocessing reaction process R4 employs a fixed bed hydroprocessing mode to complete hydrocracking reaction of more than 80% of the hydrocarbon components having a conventional boiling point greater than 280°C in the reaction feedstock oil.

[0302] Generally, the naphtha obtained from separation of the fourth hydroprocessing generated oil is subjected to catalytic reforming reaction process to produce aromatic hydrocarbons;

[0303] The hydrogen-rich gas obtained from the gaseous product of the catalytic reforming process is introduced into the first hydroprocessing reaction process R1 and / or the second hydroprocessing reaction process R2 and / or the third hydroprocessing reaction process R3 and / or the fourth hydroprocessing reaction process R4.

[0304] Generally, the heavy hydrocarbon is a low hydrogen content heavy hydrocarbon having a hydrogen content of less than 9 wt% of the hydrocarbons having a conventional boiling point higher than 450°C;

[0305] The medium hydrocarbon is a low hydrogen content medium hydrocarbon having a hydrogen content of less than 10.5 wt% of the hydrocarbons having a conventional boiling point lower than 515°C.

[0306] Generally, the heavy hydrocarbon is a low hydrogen content heavy hydrocarbon having a hydrogen content of less than 7.5 wt% of the hydrocarbons having a conventional boiling point higher than 450°C;

[0307] The medium hydrocarbon is a low hydrogen content medium hydrocarbon having a hydrogen content of less than 9.0 wt% of the hydrocarbons having a conventional boiling point lower than 515°C.

[0308] The low hydrogen content heavy hydrocarbon and the low hydrogen content medium hydrocarbon can be obtained from a fractionation process of an initial coal tar;

[0309] In the initial coal tar fractionation process, the initial coal tar is fractionated into several narrow fraction oils with different boiling ranges, the fractionation bottom oil mainly composed of hydrocarbons with conventional boiling points higher than 450℃ and containing asphaltene is used as heavy hydrocarbon with low hydrogen content, the distillate oil mainly composed of hydrocarbons with conventional boiling points lower than 450℃ is used as medium hydrocarbon with low hydrogen content; the distillate oil mainly composed of C5-C11 hydrocarbons is sent to the third hydrogenation reaction process R3.

[0310] In the present application, the heavy hydrocarbon with low hydrogen content and the medium hydrocarbon with low hydrogen content can come from the fractionation process of the initial medium-low temperature coal tar, and the fractionation process of the initial coal tar simultaneously obtains the narrow fraction distillate oil rich in phenols as phenolic oil.

[0311] The dephenolized oil obtained after the phenolic oil is dephenolized is sent to the second hydrogenation reaction process R2 or the third hydrogenation reaction process R3.

[0312] In the present application, generally, the heavy hydrocarbon with low hydrogen content and the medium hydrocarbon with low hydrogen content can come from the fractionation process of the initial medium-low temperature coal tar.

[0313] Before the initial medium-low temperature coal tar is sent to the fractionation process of the initial medium-low temperature coal tar, one or more of the following processes is completed:

[0314] ① a dehydration process;

[0315] ② a mechanical impurity removal process;

[0316] ③ a coke powder removal process;

[0317] ④ a desalination process to remove at least part of organic metal;

[0318] ⑤ an extraction separation process to remove at least part of asphaltene.

[0319] In the present application, the fourth hydrogenation reaction product R4P can be separated into hot high-pressure gas TS4V and hot high-pressure liquid TS4L in a hot high-pressure separation process TS4.

[0320] Based on the hot high-pressure gas TS4V, cold high-pressure gas CS4V and cold high-pressure liquid CS4L are separated in a cold high-pressure separation process CS4.

[0321] The separation and fractionation process of the third hydrogenation product S3L is partially or wholly combined with the separation and fractionation process of the cold high-pressure liquid CS4L.

[0322] The separation and fractionation process of the hot high-pressure liquid TS4L is not combined with the separation and fractionation process of the third hydrogenation product S3L and the cold high-pressure liquid CS4L.

[0323] Generally, the present invention uses a boiling bed hydrogenation reactor in the hydrogenation reaction process RB and uses a fixed bed hydrogenation reactor upstream and / or downstream of the boiling bed hydrogenation reactor.

[0324] Generally, the present invention uses a hydrocracking catalyst and a hydrofining catalyst in the fourth hydrogenation reaction process R4, and the hydrofining catalyst bed is upstream and / or downstream of the hydrocracking catalyst bed.

[0325] Generally, the present invention uses one or two or more catalysts in series in the second hydrogenation reaction process R2.

[0326] Generally, the fourth hydrogenation product R4P can be separated into a hot gas fraction TS4V rich in carbon 6 to carbon 8 components and a hot gas oil TS4L in the fourth hot high pressure separation process TS4 with or without stripping hydrogen gas.

[0327] At least part of the hydrocarbon stream based on the hot gas oil TS4L is recycled to the fourth hydrogenation reaction process R4 for hydrocracking reaction.

[0328] Generally, the present invention uses the following path for the part of the high pressure recycle oil TS4LR to be recycled to the fourth hydrogenation reaction process R4 for hydrocracking reaction.

[0329] The recycle oil is cooled by the heat exchanger HX and returned to the inlet of the catalyst bed in the rear part of the fourth hydrogenation reaction process R4 to act as a cooling medium to reduce the amount of quenching recycle hydrogen.

[0330] The heat exchanger HX can be used to preheat the hydrocarbon material for the fractionation process of the fourth hydrogenation product oil.

[0331] The following describes the general control principle of the gas phase hydrogen sulfide concentration of the hydrogenation reaction process of the present invention.

[0332] For the heavy oil slurry bed hydrocracking process with high nitrogen content and low sulfur content, in order to maintain the minimum hydrogen sulfide partial pressure of the initial reaction process, as needed, any kind of supplemental sulfur can be added to any hydrogenation reaction process, but generally added to the inlet of the most upstream hydrogenation reaction process to ensure that the minimum hydrogen sulfide concentration required by the reaction process, such as 500 ppm(v) or 1000 ppm(v) or 3000 ppm(v) or other expected specified value, to ensure that the hydrogen sulfide partial pressure required by the catalyst is not lower than the minimum specified value, to ensure the sulfurization type required by the catalyst. The supplemental sulfur can be hydrogen sulfide or a material that can be converted into hydrogen sulfide without adversely affecting the hydroconversion process, such as hydrogen sulfide-containing gas or oil, or liquid sulfur or carbon disulfide or dimethyl disulfide that generates hydrogen sulfide after contacting with high temperature hydrogen.

[0333] The following describes the general principles of the high pressure separation process of the hydrogenation reaction effluent.

[0334] The high pressure separation process of the hydrogenation reaction effluent usually comprises a cold high pressure separator. When the density of the hydrocarbon oil in the hydrogenation reaction effluent is large (such as close to the density of water) or the viscosity is large or it is difficult to separate from water emulsion or contains solid particles, a hot high pressure separator with an operating temperature of usually 150-450°C is also required, in which case the hydrogenation reaction effluent enters the hot high pressure separator to separate into a hot high separation gas mainly composed of hydrogen gas in volume and a hot high separation oil liquid mainly composed of conventional liquid hydrocarbon and possibly existing solid, the hot high separation gas enters the cold high pressure separator with an operating temperature of usually 20-80°C to separate into cold high separation oil and cold high separation gas. Due to the large amount of high boiling point components entering the hot high separation oil liquid, the following objectives are achieved: the density of the cold high separation oil becomes smaller or the viscosity becomes smaller or it is easy to separate from water. The high pressure separation process of the hydrogenation reaction effluent is provided with a hot high pressure separator, which also has the advantage of reducing heat loss, because the hot high separation oil liquid can avoid the cooling process of the hot high separation gas using air coolers or water coolers. At the same time, part of the hot high separation oil liquid can be returned to the upstream hydrogenation reaction process for recycling to improve the overall feedstock properties of the hydrogenation reaction process receiving the recycled oil, or the recycled hot high separation oil is subjected to cyclic hydrogenation.

[0335] Between the hot high pressure separation part and the cold high pressure separation part, a warm high pressure separation part can be provided as needed, in which case the hot high separation gas is cooled to become a gas-liquid two-phase material, which is separated in the warm high pressure separator into a warm high separation gas mainly composed of hydrogen gas in volume and a warm high separation oil liquid mainly composed of conventional liquid hydrocarbon and possibly existing solid, and the warm high separation gas enters the cold high pressure separation part for cooling and gas-liquid separation.

[0336] The hydrogenation reaction effluent or hot high pressure gas or warm high pressure gas is usually cooled (usually by heat exchange with the feed to the reaction section) to a temperature of about 220 to 100°C (the temperature should be higher than the crystallization temperature of ammonium hydrosulfide and the crystallization temperature of ammonium chloride in the gas phase of the hydrogenation reaction effluent) before it enters the cold high pressure separation section. Then, usually, water is injected into the hydrogenation reaction effluent to form a water injected hydrogenation reaction effluent. Two or more injection points can be provided. The water is used to absorb ammonia and other impurities such as hydrogen chloride which can be produced. The water solution after absorbing ammonia will absorb hydrogen sulfide. In the cold high pressure separation section, the water injected hydrogenation reaction effluent is separated into a cold high pressure gas which is mainly hydrogen in volume, a cold high pressure liquid which is mainly conventional liquid hydrocarbons and dissolved hydrogen, and a cold high pressure water which is mainly water and dissolves ammonia and hydrogen sulfide. The ammonia content in the cold high pressure water is usually 0.5 to 15% (w) and preferably 1 to 8% (w). One of the purposes of injecting water is to absorb ammonia and hydrogen sulfide in the hydrogenation reaction effluent to prevent the formation of ammonium hydrosulfide or polysulfide which can crystallize and plug the heat exchanger channels and increase the pressure drop of the system. The amount of water injected should be determined according to the following principles: on the one hand, the water injected into the hydrogenation reaction effluent is separated into a vapor phase and a liquid phase, and the amount of the liquid phase must be greater than zero and preferably 30% or more of the total amount of water; on the other hand, the water is used to absorb ammonia in the hydrogenation reaction effluent to prevent the ammonia concentration in the high pressure gas from being too high and reducing the activity of the catalyst. The ammonia concentration in the high pressure gas is usually lower the better and is usually not more than 200 ppm (v) and preferably not more than 50 ppm (v). The operating pressure of the cold high pressure separator is the pressure of the hydrogenation reaction section minus the actual pressure drop. The difference between the operating pressure of the cold high pressure separation section and the pressure of the hydrogenation reaction section should not be too low or too high and is usually 0.35 to 3.2 MPa and usually 0.5 to 1.5 MPa. The hydrogen concentration in the cold high pressure gas should not be too low (which will cause the operating pressure of the unit to rise) and is usually not less than 70% (v), preferably not less than 80% (v) and most preferably not less than 85% (v). As mentioned before, at least a part of the cold high pressure gas, usually 85 to 100%, is recycled to the hydrogenation reaction section to provide the necessary hydrogen and hydrogen concentration in the hydrogenation reaction section. In order to improve the efficiency of the investment, the concentration of the recycled hydrogen must be not less than the lower limit mentioned before. Therefore, according to the properties of the specific feedstock, the reaction conditions and the product distribution, a part of the cold high pressure gas can be removed to remove the methane and ethane produced in the reaction. The removed cold high pressure gas can be separated into hydrogen and non-hydrogen components by using a conventional membrane separation process or a pressure swing adsorption process or an oil washing process, and the recovered hydrogen can be used as fresh hydrogen.

[0337] For heavy oil slurry-bed hydrocracking process, because of the huge production of CH4, C2H6, H2S, usually part or all of the cold high pressure gas, such as about 30-100% of the cold high pressure gas, is purified by membrane separation process, and the permeated hydrogen is pressurized and returned to the hydrogenation reaction process, and the unpermeated gas can be pressurized and returned to the hydrogenation reaction process after PSA hydrogen extraction or after "steam reforming hydrogen production + PSA hydrogen extraction".

[0338] New hydrogen enters the hydrogenation part to supplement the hydrogen consumed by the hydrogenation reaction process, and the higher the hydrogen concentration of the new hydrogen is, the better, and generally it should not be lower than 95%(v), and preferably not lower than 99%(v). All new hydrogen can be introduced into any hydrogenation reaction part, and preferably introduced into the first hydrogenation reactor.

[0339] In the present application, the hydrogen stream used in any reaction process can be all new hydrogen, all recycled hydrogen, or a mixture of new hydrogen and recycled hydrogen.

Claims

1. A combined hydroconversion process of heavy hydrocarbon, medium hydrocarbon using hydrogen in tertiary series, comprising the following processes: heavy hydrocarbon RAF, mainly composed of hydrocarbon components with conventional boiling point higher than 450℃ and containing at least a part of asphaltene components with conventional boiling point higher than 510℃; medium hydrocarbon RBF, mainly composed of conventional liquid hydrocarbon with conventional boiling point lower than 510℃; first hydroconversion product R1P produced by hydrogen-rich gas through first hydroconversion process R1, separated into hot high-pressure gas S1V and hot high-pressure liquid S1L through first hot high-pressure separation process S1; second hydroconversion product R2P produced by hydrogen-rich stream based on hot high-pressure gas S1V through second hydroconversion process R2, separated into hot high-pressure gas S2V and hot high-pressure liquid S2L through second hot high-pressure separation process S2; third hydroconversion product R3P produced by hydrogen-rich stream based on hot high-pressure gas S2V through third hydroconversion process R3, separated into hydrogen-rich third separation gas S3V and third hydroconversion oil S3L through third separation process S3; at least a part of third separation gas S3V recycled to first hydroconversion process R1 and / or second hydroconversion process R2 and / or third hydroconversion process R3; heavy hydrocarbon RAF subjected to hydro-lightrization reaction in hydroconversion process RA, and heavy hydrocarbon hydroconversion product RAP separated into hot high-pressure gas SAV and hot high-pressure liquid SAL through hot high-pressure separation process SA; hydroconversion process RA, with or without hydrogen-donating hydrocarbon stream; medium hydrocarbon RBF subjected to hydro-treatment reaction in hydroconversion process RB, and medium hydrocarbon hydro-treatment product RBP separated into hot high-pressure gas SBV and hot high-pressure liquid SBL through hot high-pressure separation process SB; when hydroconversion process RA is carried out in first hydroconversion process R1, hydroconversion process RB is carried out in second hydroconversion process R2, at this time, hot high-pressure gas SAV is hot high-pressure gas S1V, hot high-pressure liquid SAL is hot high-pressure liquid S1L, hot high-pressure gas SBV is hot high-pressure gas S2V, and hot high-pressure liquid SBL is hot high-pressure liquid S2L; or when hydroconversion process RB is carried out in first hydroconversion process R1, hydroconversion process RA is carried out in second hydroconversion process R2, at this time, hot high-pressure gas SBV is hot high-pressure gas S1V, hot high-pressure liquid SBL is hot high-pressure liquid S1L, hot high-pressure gas SAV is hot high-pressure gas S2V, and hot high-pressure liquid SAL is hot high-pressure liquid S2L; stream based on hot high-pressure liquid SAL separated into residue oil SAL-H mainly composed of hydrocarbon with conventional boiling point higher than 515℃, distillate oil SAL-M mainly composed of hydrocarbon with conventional boiling point 50-515℃ and gas after pressure reduction; at least a part of distillate oil SAL-LM enters hydroconversion process RB and / or third hydroconversion process R3.

2. The method according to claim 1, characterized in that: ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ The separation of the stream after pressure reduction based on thermal high- resolution SAL is into a residue oil SAL-H mainly composed of hydrocarbons with a conventional boiling point higher than 515°C, a distillate oil SAL-M1 mainly composed of hydrocarbons from carbon 12 to 515°C, a distillate oil SAL-M2 mainly composed of hydrocarbons from carbon 5 to carbon 11, and a gas; Part of the residue oil SAL-H is recycled to the hydrogenation reaction process RA; At least part of the distillate oil SAL-M1 is introduced into the hydrogenation reaction process RB; At least part of the distillate oil SAL-M2 is introduced into the third hydrogenation reaction process R3.

3. The method according to claim 1, wherein: the thermal hydrocarbon oil processing process is selected from a hydrocarbon oil coking process or / and a hydrocarbon oil catalytic cracking process and / or a hydrocarbon oil catalytic pyrolysis process; the heavy hydrocarbon RAF is selected from one or more of the following: ① a low-temperature coal tar heavy oil fraction and a heavy oil fraction obtained by thermal processing thereof; ② a medium-temperature coal tar heavy oil fraction and a heavy oil fraction obtained by thermal processing thereof; ③ a high-temperature coal tar heavy oil fraction and a heavy oil fraction obtained by thermal processing thereof; ④ a petroleum-based heavy oil and a heavy oil fraction product obtained by thermal processing thereof; ⑤ a shale oil-based heavy oil and a heavy oil fraction product obtained by thermal processing thereof; and ⑥ a petroleum sand-based heavy oil and a heavy oil fraction product obtained by thermal processing thereof; and the medium hydrocarbon RBF is selected from one or more of the following: ① a low-temperature coal tar medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; ② a medium-temperature coal tar medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; ③ a high-temperature coal tar medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; ④ a petroleum-based medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; ⑤ a shale oil medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; and ⑥ a petroleum sand-based medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof.

4. The method according to claim 2, wherein: the thermal hydrocarbon oil processing process is selected from a hydrocarbon oil coking process or / and a hydrocarbon oil catalytic cracking process and / or a hydrocarbon oil catalytic pyrolysis process; the heavy hydrocarbon RAF is selected from one or more of the following: ① a low-temperature coal tar heavy oil fraction and a heavy oil fraction obtained by thermal processing thereof; ② a medium-temperature coal tar heavy oil fraction and a heavy oil fraction obtained by thermal processing thereof; ③ a high-temperature coal tar heavy oil fraction and a heavy oil fraction obtained by thermal processing thereof; ④ a petroleum-based heavy oil and a heavy oil fraction product obtained by thermal processing thereof; ⑤ a shale oil-based heavy oil and a heavy oil fraction product obtained by thermal processing thereof; and ⑥ a petroleum sand-based heavy oil and a heavy oil fraction product obtained by thermal processing thereof; and the medium hydrocarbon RBF is selected from one or more of the following: ① a low-temperature coal tar medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; ② a medium-temperature coal tar medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; ③ a high-temperature coal tar medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; ④ a petroleum-based medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; ⑤ a shale oil medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof; and ⑥ a petroleum sand-based medium distillate oil and a hydrocarbon oil obtained by thermal processing thereof.

5. The method according to claim 1, wherein: ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ ​ The hot high pressure liquid SBL is fed into the fourth hydroprocessing reaction process R4 containing at least hydrocracking function to produce a fourth hydroprocessing reaction product R4P, and the fourth hydroprocessing reaction product R4P is separated to produce a fourth hydrogen rich gas V40 and a fourth hydroprocessing oil L40, and at least part of the fourth hydrogen rich gas V40 is recycled back to the fourth hydroprocessing reaction process R4.

6. The method according to claim 5, wherein: The hot high pressure liquid SBL is fed into the fourth hydroprocessing reaction process R4 at a pressure as close as possible to the operating pressure of the hot high pressure liquid SBL.

7. The method according to claim 5, wherein: The separation process of the third hydroprocessing oil S3L and the separation process of the fourth hydroprocessing oil L40 are partially or totally shared.

8. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, wherein: The recycle oil RO-TORA used in the hydroprocessing reaction process RA is recycled back to the hydroprocessing reaction process RA; The recycle oil RO-TORA is selected from one or more of the following: ① a separated liquid obtained by separating an intermediate product or a final product of the hydroprocessing reaction process RA; ② at least part of the hot high pressure liquid SAL; ③ a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point greater than 515℃ obtained by separating the hot high pressure liquid SAL; ④ a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point greater than 350℃ obtained by separating the hot high pressure liquid SAL; ⑤ a distillate oil mainly composed of hydrocarbons with a conventional boiling point greater than 220℃ obtained by separating the hot high pressure liquid SAL; ⑥ a separated liquid obtained by separating an intermediate product or a final product of the hydroprocessing reaction process RB, and recycled back to the hydroprocessing reaction process RA; ⑦ part of the hot high pressure liquid SBL; ⑧ a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point greater than 515℃ obtained by separating the hot high pressure liquid SBL; ⑨ a hydrocarbon liquid mainly composed of hydrocarbons with a conventional boiling point greater than 220℃ obtained by separating an intermediate product or a final product of the fourth hydroprocessing reaction process R4; ⑩ a hydrocarbon liquid mainly composed of hydrocarbons with a conventional boiling point greater than 350℃ obtained by separating an intermediate product or a final product of the fourth hydroprocessing reaction process R4; separating the product of the fourth hydrogenation reaction process R4 to obtain a hot high-pressure separation process separation liquid; The recycle oil RO-TORA is used as a heat carrying oil to carry the reaction heat or as a hydrogen containing hydrocarbon stream to supply hydrogen, and the recycle oil RO-TORA or the recycle oil RO-TORA is mixed with an intermediate product of the hydroprocessing reaction process RA and the heavy hydrocarbon RAF or an intermediate hydroprocessing product of the heavy hydrocarbon RAF.

9. The method according to claim 8, wherein: In the hydroprocessing reaction process RA, the ratio of the weight flow rate of the recycle oil RO-TORA to the weight flow rate of the heavy hydrocarbon RAF is K100, and K100 is selected from one of the following: ①0.01～0.20； ②0.20～0.80； ③0.80～2.00； ④2.00～10.00。 10. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, wherein: The recycle oil RO-TORB used in the hydroprocessing reaction process RB is recycled back to the hydroprocessing reaction process RB; The recycle oil RO-TORB is selected from one or more of the following: ① a separated liquid obtained by separating an intermediate product or a final product of the hydroprocessing reaction process RB; ② part of the hot high pressure liquid SBL; ③ separating the stream based on the thermal high pressure separation of the SBL to obtain a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point greater than 350℃; ④ separating the fourth hydrogenation reaction product R4P to obtain a distillate oil mainly composed of hydrocarbons with a conventional boiling point of 220-515℃; ④ separating the intermediate product or the final product of the fourth hydrogenation reaction process R4 to obtain a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point of 220-515℃; ⑤ separating the intermediate product or the final product of the fourth hydrogenation reaction process R4 to obtain a hydrocarbon oil mainly composed of hydrocarbons with a conventional boiling point of 330-515℃; ⑥ separating the product of the fourth hydrogenation reaction process R4 to obtain a separation liquid of the thermal high pressure separation process.

11. The method according to claim 10, wherein: In the hydrogenation reaction process RB, the ratio of the weight flow rate of the recycle oil RO-TORB to the weight flow rate of the medium hydrocarbon RBF is K200, and K200 is selected from one of the following: ①0.20～0.80； ②0.80～2.00； ③2.00～10.00。 12. The method according to claim 5 or 6, wherein: The fourth hydrogenation reaction process R4 uses the recycle oil RO-TOR4 to return to the fourth hydrogenation reaction process R4 for recycling reaction; The recycle oil RO-TOR4 is selected from one or more of the following: ① separating the intermediate product or the final product of the fourth hydrogenation reaction process R4 to obtain a hydrocarbon liquid mainly composed of hydrocarbons with a conventional boiling point greater than 220℃; ② separating the intermediate product or the final product of the fourth hydrogenation reaction process R4 to obtain a hydrocarbon liquid mainly composed of hydrocarbons with a conventional boiling point greater than 350℃; ③ separating the intermediate product or the final product of the fourth hydrogenation reaction process R4 to obtain a hydrocarbon liquid mainly composed of hydrocarbons with a conventional boiling point greater than 350℃; ④ separating the product of the fourth hydrogenation reaction process R4 to obtain a separation liquid of the thermal high pressure separation process.

13. The method according to claim 12, wherein: In the fourth hydrogenation reaction process R4, the ratio of the weight flow rate of the recycle oil RO-TOR4 to the weight flow rate of the fresh conventional liquid hydrocarbon feed R7F of the fourth hydrogenation reaction process R4 is K700, and K700 is selected from one of the following: ①0.20～0.80； ②0.80～2.00。 14. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, wherein: The heavy hydrocarbon RAF and the medium hydrocarbon RB are from a distillation process of a medium-low temperature coal tar; The hydrogenation reaction process RA performs a hydro-lightration reaction of the heavy hydrocarbon RAF, using a suspension bed hydrogenation reaction mode or a boiling bed hydrogenation reaction mode, with or without a hydrogen-donor solvent; the cracking conversion rate of the hydrocarbon components with a conventional boiling point greater than 515℃ in the heavy hydrocarbon RAF is higher than 55wt%; A fractionation bottom oil mainly composed of hydrocarbon components with a conventional boiling point higher than 515℃ is separated from the oil generated by the hydrogenation reaction process RA, and is partially returned to the hydrogenation reaction process RA; The hydrogenation reaction process RB performs a hydro-treatment reaction of the medium hydrocarbon RAF, using a boiling bed hydrogenation reaction mode and / or a fixed bed hydrogenation reaction mode, and at least 50wt% of the hydrogenation desulfurization reaction and 50wt% of the hydrogenation denitrification reaction are completed; The hydrogenation reaction process RB includes a boiling bed hydrogenation reaction mode, and the oil generated by separating the hydrogenation reaction process RB is mainly composed of hydrocarbon components with a conventional boiling point higher than 350℃, and is partially returned to the hydrogenation reaction process RB; The third hydrogenation reaction process R3 is a fixed bed hydrogenation reaction mode, and at least 50wt% of the hydrogenation desulfurization reaction and 50wt% of the hydrogenation denitrification reaction are completed.

15. The method according to claim 14, wherein: The hydrogenation reaction process RA has a cracking conversion rate of hydrocarbon components with a conventional boiling point higher than 515℃ in the heavy hydrocarbon RAF higher than 85wt%; The hydrogenation reaction process RB at least completes 95wt% of the hydrogenation desulfurization reaction and 95wt% of the hydrogenation denitrification reaction; The third hydrogenation reaction process R3 at least completes 95wt% of the hydrogenation desulfurization reaction and 95wt% of the hydrogenation denitrification reaction; The fourth hydrogenation reaction process R4 is a fixed bed hydrogenation reaction mode, and at least 90wt% of the hydrocracking reaction of hydrocarbon components with a conventional boiling point higher than 350℃ in the reaction raw oil is completed.

16. The method according to claim 15, wherein: The fourth hydrogenation reaction process R4 has a flow rate of hydrocarbon components with carbon 6 to carbon 8 in the fourth hydrogenation reaction oil higher than 40wt% of the flow rate of the fresh raw material oil of the fourth hydrogenation reaction process R4.

17. The method according to claim 15, wherein: The fourth hydrogenation reaction process R4 has a flow rate of hydrocarbon components with carbon 6 to carbon 8 in the fourth hydrogenation reaction oil higher than 55wt% of the flow rate of the fresh raw material oil of the fourth hydrogenation reaction process R4.

18. The method according to claim 14, wherein: The heavy hydrocarbon with low hydrogen content is a fractionation bottom oil from a fractionation process based on a medium-low temperature coal tar material, mainly composed of hydrocarbon components with a conventional boiling point higher than 450℃ and containing asphaltene; The medium hydrocarbon with low hydrogen content is a distillate oil from a fractionation process based on a medium-low temperature coal tar material and having a carbon residue content lower than 1wt%; The hydrogenation reaction process RA is a slurry bed hydrocracking reaction process, and the operating conditions are: a temperature of 380-450℃, a pressure of 8.0-25.0MPa, and the slurry bed hydrogenation catalyst of the hydrogenation reaction process RA at least contains molybdenum sulfide microcrystals, the proportion of the molybdenum sulfide microcrystals is 0.050wt%-0.500wt% of the hydrocarbon oil in the reaction liquid phase, the amount of organic metal in the net generated oil of the hydrogenation reaction process RA is lower than 90wt% of the amount of organic metal in the fresh raw material hydrocarbon of the hydrogenation reaction process RA, and the carbon residue amount in the net generated oil of the hydrogenation reaction process RA is lower than 50% of the carbon residue amount in the fresh raw material hydrocarbon of the hydrogenation reaction process RA; The operating conditions of the thermal high-pressure separation process SA are: a temperature of 200-450℃, a pressure of 8.0-25.0MPa, and the volume concentration of hydrogen in the first separation gas S1V is higher than 65vol%. The hydrogenation reaction process RB uses a boiling bed hydrogenation reactor with or without a fixed bed hydrogenation reactor, and the operating conditions are: temperature 230-450℃, pressure 8.0-25.0MPa; the boiling bed hydrogenation reactor used by the hydrogenation reaction process RB has an expansion ratio of 1.12-1.55 for the boiling bed hydrogenation catalyst bed, the amount of organic metal in the net generated oil of the hydrogenation reaction process RB is less than 10wt% of the amount of organic metal in the fresh raw hydrocarbon of the second hydrogenation reaction process R2, the amount of residual carbon in the net generated oil of the hydrogenation reaction process RB is less than 30wt% of the amount of residual carbon in the fresh raw hydrocarbon of the hydrogenation reaction process RB, the amount of organic sulfur in the net generated oil of the hydrogenation reaction process RB is less than 10wt% of the amount of organic sulfur in the fresh raw hydrocarbon of the hydrogenation reaction process RB, and the amount of organic nitrogen in the net generated oil of the hydrogenation reaction process RB is less than 20wt% of the amount of organic nitrogen in the fresh raw hydrocarbon of the hydrogenation reaction process RB; The operating conditions of the hot high-pressure separation process SB are: temperature 200-450℃, pressure 8.0-25.0MPa, and the volume concentration of hydrogen in the second separation gas S2V is higher than 65vol%; The third hydrogenation reaction process R3 is a hydroprocessing reaction process, and the operating conditions are: temperature 230-450℃, pressure 8.0-25.0MPa, the amount of organic metal in the net generated oil of the third hydrogenation reaction process R3 is less than 10ppm, the amount of organic nitrogen in the net generated oil of the third hydrogenation reaction process R3 is less than 100ppm, and the amount of organic nitrogen in the net generated oil of the third hydrogenation reaction process R3 is less than 50ppm; The volume concentration of hydrogen in the third hydrogen-rich gas is greater than 65%.

19. The method of claim 18, wherein: The operating conditions of the hydrogenation reaction process RA are: temperature 400-440℃, pressure 10.0-18.0MPa, and the amount of residual carbon in the net generated oil of the hydrogenation reaction process RA is less than 80% of the amount of residual carbon in the fresh raw hydrocarbon of the hydrogenation reaction process RA; The operating conditions of the hot high-pressure separation process SA are: temperature 400-440℃, pressure 10.0-18.0MPa, and the volume concentration of hydrogen in the first separation gas S1V is higher than 75vol%; The operating conditions of the hydrogenation reaction process RB are: temperature 230-450°C, pressure 10.0-18.0 MPa; the boiling bed hydrogenation reactor used in the hydrogenation reaction process RB, the expansion ratio of the boiling bed hydrogenation catalyst bed is 1.2-1.4, the organic metal amount in the net generated oil of the hydrogenation reaction process RB is less than 5% of the organic metal amount in the fresh raw material hydrocarbon of the second hydrogenation reaction process R2, the residual carbon amount in the net generated oil of the hydrogenation reaction process RB is less than 10% of the residual carbon amount in the fresh raw material hydrocarbon of the hydrogenation reaction process RB, the organic sulfur content in the net generated oil of the hydrogenation reaction process RB is less than 5% by weight of the organic sulfur content in the fresh raw material hydrocarbon of the hydrogenation reaction process RB, the organic nitrogen content in the net generated oil of the hydrogenation reaction process RB is less than 5% by weight of the organic nitrogen content in the fresh raw material hydrocarbon of the hydrogenation reaction process RB; The operating conditions of the thermal high-pressure separation process SB are: temperature 200-450°C, pressure 10.0-18.0 MPa, the volume concentration of hydrogen in the second separation gas S2V is higher than 75% by volume; The third hydrogenation reaction process R3 is a hydrotreating reaction process, the operating conditions are: temperature 230-450°C, pressure 8.0-25.0 MPa, the organic metal amount in the net generated oil of the third hydrogenation reaction process R3 is less than 2 ppm, the organic sulfur content in the net generated oil of the third hydrogenation reaction process R3 is less than 10 ppm, the organic nitrogen content in the net generated oil of the third hydrogenation reaction process R3 is less than 2 ppm; The volume concentration of hydrogen in the third hydrogen-rich gas is greater than 75%.

20. The method according to claim 5 or 6, wherein: The fourth hydrogenation reaction process R4 uses a fixed bed hydrogenation reaction mode, and at least 50% by weight of the hydrocarbon components with a conventional boiling point greater than 350°C in the reaction raw material oil is subjected to hydrocracking reaction; The fractionated bottom oil containing hydrocarbon components with a conventional boiling point higher than 350°C obtained by separating the generated oil of the fourth hydrogenation reaction process R4 is at least partially returned to the fourth hydrogenation reaction process R4.

21. The method according to claim 5 or 6, wherein: The fourth hydrogenation reaction process R4 uses a fixed bed hydrogenation reaction mode, and at least 70% by weight of the hydrocarbon components with a conventional boiling point greater than 350°C in the reaction raw material oil is subjected to hydrocracking reaction; The hydrocarbon oil containing hydrocarbon components with a conventional boiling point higher than 220°C obtained by separating the generated oil of the fourth hydrogenation reaction process R4 is at least partially returned to the fourth hydrogenation reaction process R4 to produce more carbon 6-carbon 8 hydrocarbons.

22. The method according to claim 5 or 6, wherein: The fourth hydrogenation reaction process R4, the organic metal amount in the net generated oil is less than 2 ppm, the organic sulfur content in the net generated oil is less than 2 ppm, and the organic nitrogen content in the net generated oil is less than 10 ppm.

23. The method according to claim 22, wherein: The fourth hydrogenation reaction process R4 uses a fixed bed hydrogenation reaction mode, and all the hydrocarbon components with a conventional boiling point greater than 350°C in the reaction raw material oil are subjected to hydrocracking reaction; The fourth hydroprocessing reaction process R4, using fixed bed hydroprocessing reaction mode, more than 80% of the hydrocarbon components with conventional boiling point higher than 280℃ in the reaction feedstock oil complete hydrocracking reaction.

24. The method according to claim 5 or 6, wherein: The naphtha obtained from the separation of the fourth hydroprocessing product oil is sent to a catalytic reforming reaction process to produce aromatic hydrocarbons; The hydrogen-rich gas obtained from the gaseous product of the catalytic reforming process is sent to the first hydroprocessing reaction process R1 and / or the second hydroprocessing reaction process R2 and / or the third hydroprocessing reaction process R3 and / or the fourth hydroprocessing reaction process R4.

25. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, wherein: The heavy hydrocarbon is a low hydrogen content heavy hydrocarbon, wherein the hydrogen content of the hydrocarbon with conventional boiling point higher than 450℃ is less than 9wt%; The medium hydrocarbon is a low hydrogen content medium hydrocarbon, wherein the hydrogen content of the hydrocarbon with conventional boiling point lower than 515℃ is less than 10.5wt%.

26. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, wherein: The heavy hydrocarbon is a low hydrogen content heavy hydrocarbon, wherein the hydrogen content of the hydrocarbon with conventional boiling point higher than 450℃ is less than 7.5wt%; The medium hydrocarbon is a low hydrogen content medium hydrocarbon, wherein the hydrogen content of the hydrocarbon with conventional boiling point lower than 515℃ is less than 9.0wt%.

27. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7, wherein: The low hydrogen content heavy hydrocarbon and the low hydrogen content medium hydrocarbon are obtained from a fractionation process of the initial coal tar; In the fractionation process of the initial coal tar, the initial coal tar is fractionated into several narrow fraction oils with different boiling ranges, the fractionation bottom oil mainly composed of hydrocarbons with conventional boiling point higher than 450℃ and containing asphaltene is used as the low hydrogen content heavy hydrocarbon, the distillate oil mainly composed of hydrocarbons with conventional boiling point lower than 450℃ is used as the low hydrogen content medium hydrocarbon, and the distillate oil mainly composed of hydrocarbons with carbon number from 5 to 11 is sent to the third hydroprocessing reaction process R3 with or without.

28. The method according to claim 27, wherein: The low hydrogen content heavy hydrocarbon and the low hydrogen content medium hydrocarbon are obtained from a fractionation process of the initial medium-low temperature coal tar, and the fractionation process of the initial coal tar simultaneously obtains a narrow fraction distillate oil rich in phenols as a phenol oil; The dephenolized oil obtained after the phenol oil is dephenolized is sent to the second hydroprocessing reaction process R2 or the third hydroprocessing reaction process R3.

29. The method according to claim 27, wherein: The low hydrogen content heavy hydrocarbon and the low hydrogen content medium hydrocarbon are obtained from a fractionation process of the initial medium-low temperature coal tar; Before the initial medium-low temperature coal tar is sent to the fractionation process of the initial medium-low temperature coal tar, one or more of the following processes are completed: ① a dehydration process; ② a mechanical impurity removal process; ③ a coke powder removal process; ④ a desalting process to remove at least a part of organic metal; ⑤ an extraction separation process to remove at least a part of asphaltene.

30. The method according to claim 5 or 6, wherein: The fourth hydroprocessing reaction product R4 is separated into a hot high pressure vapor TS4V and a hot high pressure liquid TS4L in a hot high pressure separation process TS4. The hot gas TS4V is separated from the hot gas TS4L in a fourth hot high pressure separation process TS4. The separation and fractionation process of the third hydrogenation product S3L is partially or wholly combined with the separation and fractionation process of the cold high separation liquid CS4L. The separation and fractionation process of the hot high separation liquid TS4L is not combined with the separation and fractionation process of the third hydrogenation product S3L and the cold high separation liquid CS4L.

31. The method of claim 1, wherein: The hydrogenation reaction process RB uses a ebullated bed hydrogenation reactor and uses a fixed bed hydrogenation reactor upstream and / or downstream of the ebullated bed hydrogenation reactor.

32. The method of claim 5 or 6, wherein: In the fourth hydrogenation reaction process R4, a hydrocracking catalyst and a hydrofining catalyst are used, and the hydrofining catalyst bed is upstream and / or downstream of the hydrocracking catalyst bed.

33. The method of claim 1 or 2 or 3 or 4 or 5 or 6 or 7, wherein: In the second hydrogenation reaction process R2, the hydrogenation catalyst used is a series combination of one or two or more catalysts.

34. The method of claim 1, wherein: The fourth hydrogenation product R4P is separated into the hot gas TS4V rich in C6-C8 components and the hot oil TS4L in a fourth hot high pressure separation process TS4 with or without stripping hydrogen gas. At least part of the hot oil TS4L is recycled back to the fourth hydrogenation reaction process R4 for hydrocracking reaction.

35. The method of claim 34, wherein: The path of the part of the high pressure recycle oil TS4LR recycled back to the fourth hydrogenation reaction process R4 for hydrocracking reaction is as follows: The recycle oil after being cooled by the heat exchanger HX is returned to the inlet of the rear catalyst bed of the fourth hydrogenation reaction process R4 to serve as a cooling medium to reduce the amount of quenching recycle hydrogen.

36. The method of claim 35, wherein: The heat exchanger HX is used to preheat the hydrocarbon material of the fractionation process of the fourth hydrogenation product.

Images