CN110846073B - Flushing method of main hot high-pressure oil separator containing solid product in hydrocarbon material hydrogenation process - Google Patents
Flushing method of main hot high-pressure oil separator containing solid product in hydrocarbon material hydrogenation process Download PDFInfo
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- CN110846073B CN110846073B CN201810983989.0A CN201810983989A CN110846073B CN 110846073 B CN110846073 B CN 110846073B CN 201810983989 A CN201810983989 A CN 201810983989A CN 110846073 B CN110846073 B CN 110846073B
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
Abstract
A method for flushing a main hot high-pressure oil reducer containing solid products in the hydrogenation process of hydrocarbon materials includes such steps as using flushing oil WS which is 5-20% of normal flow of hot high-pressure oil and is basically free of solid to establish soft lower limit basic flow R1 of main hot high-pressure oil reducer KV, running before coal is fed into a direct coal liquefaction reaction system R10, running after coal is fed into the system R10 normally or is stopped, when the THPSE liquid level of a hot high-pressure separator is too low and the emergency limit of KV is required to prevent the THPSE from continuously discharging liquid outwards, the lower limit position of KV opening is not zero flow and is fully closed, but a certain flow value is as small as 0.5R1-0.6R1, at this time, WS is divided into two paths, one path flows reversely and pushes hot high-pressure oil to return to the hot high-pressure separator, one path flows forward to flush solid at the sealing surface position of KV valve seat and valve core, and after the flushing process is continued for a period of time, the KV and a downstream liquid level control valve is closed again, so that the service life of the valve can be prolonged.
Description
Technical Field
The invention relates to a flushing method of a main hot high-pressure oil reducer containing solid products in a hydrocarbon hydrogenation process, which is characterized in that a soft lower limit basic flow R1 of the main hot high-pressure oil reducer KV is established by using flushing oil WS which is 5% -20% of the normal flow of the hot high-pressure oil, the main hot high-pressure oil reducer KV can be operated immediately before coal is fed into a direct coal liquefaction reaction system R10 for hydrogenation of coal, the main hot high-pressure oil reducer can be operated immediately after the coal is fed into the direct coal hydrogenation reaction system R10 or after the coal is stopped, when the THPSE liquid level of a hot high-pressure separator is too low and the emergency limit of KV is required to prevent the THPSE from continuously discharging liquid outwards, the lower limit position of the aperture of KV is not zero flow and is fully closed, but rather, a small aperture corresponding to a certain flow value such as 0.5R1-0.6R1 is adopted, at the moment, WS is divided into two paths, one path flows reversely and pushes the hot high-pressure oil to return to the hot high-pressure separator, one path flows forward to flush the solid at the sealing surface position of KV valve seat and the valve core after the flushing process lasts for a period, the time, and the downstream liquid level control valve is closed, and the service life of the valve is prolonged.
Background
The invention relates to a hydrocarbon material hydrogenation process, in particular to a coal and/or oil hydrogenation process, such as a coal hydrogenation direct liquefaction reaction process and a heavy oil hydrogenation thermal cracking reaction process.
The solid-containing hydrogenation product of the present invention is a solid particulate, most of which, such as pulverized coal, semicoke, catalyst particles, typically have a particle size of less than 200 microns, typically less than 50 microns, preferably less than 10 microns.
The main pressure reducer KV refers to a main pressure reducer KV which bears most of pressure difference in a thermal high-pressure oil-separating pressure reducing process in normal operation, the main pressure reducer KV can be 1 valve or 1 throttling pressure reducer, the main pressure reducer KV can be 2 valves or a plurality of valves or 2 throttling pressure reducers or a plurality of throttling pressure reducers, and the main pressure reducer KV can be a series or parallel operation system composed of 2 or a plurality of functional parts including the valves and the throttling pressure reducers.
The conventional process is a hot high-pressure flash evaporation separation method, and the high-pressure high-temperature solid-containing coal hydrogenation direct liquefaction reaction product enters a hot high-pressure separator THPSE to be separated into a liquid-solid mixed phase stream THPS-L containing most solid products and a hot high-pressure gas THPS-V, wherein the liquid-solid mixed phase stream THPS-L is called hot high-pressure oil THPS-L for short, and of course, the hot high-pressure oil THPS-L is a custom name well known to the person skilled in the art. In general, after the thermal high-pressure oil THPS-L is subjected to 1-stage depressurization or 2-stage depressurization or multi-stage depressurization, the thermal high-pressure oil THPS-L enters a distillation process FRAC1 to complete separation of solid and hydrocarbon components to obtain distilled oil FRAC1-MH and residues mainly composed of solid and heavy hydrocarbons, and the distilled oil FRAC1-MH is generally processed in combination with a hydrocarbon component THPS-V-LM based on thermal high-pressure gas THPS-V; the hot high-pressure oil THPS-L is extremely harsh in operation conditions for pressure reduction equipment, the operation pressure can be 18-19 MPa, the operation pressure difference can reach 14-15 MPa, the operation temperature is 400-430 ℃, high pressure and high temperature conditions enable the hot high-pressure oil to dissolve a large amount of hydrogen, about 40-60% of medium boiling point hydrocarbons such as hydrocarbons with conventional boiling point of 250-350 ℃ exist in the hot high-pressure oil in a liquid state, 6-25% of solid particles are contained, and normally the hot high-pressure oil enters a hot low-pressure separator TLPS after the pressure of the hot high-pressure oil is reduced to 2.0-6.0 MPa through a pressure reducer and is separated into hot low-pressure gas TLPS-V and hot low-pressure oil TLPS-L; the hot low-split oil TLPS-L is then further depressurized and then distilled to FRAC1.
According to the thermal high-pressure flash separation method for directly liquefying the reaction product by coal hydrogenation, the thermal high-pressure oil-separating THPS-L is a liquid-solid mixed phase material flow which is high in pressure, high in temperature, contains solid and corrosive components and contains a large amount of soluble gas and low-boiling hydrocarbon components, and the depressurization process of the thermal high-pressure oil-separating THPS-L inevitably forms strong erosion on the overflow part of the depressurization valve, so that the service life of the overflow part is seriously shortened; meanwhile, in the abrupt change process of the operation state of the THPSE, such as the initial discharging process of the initial release of the solid-containing hot high-pressure oil, the small opening valve opened by the fully closed state is actually a small flow channel flow-limiting orifice plate, and the edge of the small flow channel flow-limiting orifice plate, namely the valve sealing surface, can be rapidly eroded by the high-solid-content liquid under the drive of high pressure difference; similarly, in the abrupt change process of the operation state of the thermal high pressure separator THPSE, such as the emergency cut-off and closing process of thermal high-pressure oil separation, the small-opening valve with the normal opening rapidly reaching the closed state is actually a small-flow-channel flow-limiting orifice plate, and the edge of the small-flow-channel flow-limiting orifice plate, namely the valve sealing surface, can be rapidly eroded by the liquid with high solid content under the drive of high pressure difference; in a more dangerous situation, in the abrupt change process of the operation state of the hot high pressure separator THPSE, such as the emergency cut-off and closing process of hot high oil separation, the valve which is in a closed state rapidly reaches the normal opening, and the valve core is seated back to the valve seat sealing surface to form the closed state, so that no solid particles are possibly ensured between the closed pair of sealing surfaces, and in fact, solid particles are necessarily present, so that the sealing surfaces are extruded and damaged, that is, the valve sealing surface is damaged in the process of throwing pulverized coal each time and cutting off and closing each time, thereby shortening the service life of the valve sealing surface and being unfavorable for prolonging the continuous operation period of the device.
On the other hand, in the existing high-pressure oil reducing system for directly liquefying reaction products by coal hydrogenation, in order to make the pressure reducer in a standby state enter into an operating state, a heating program is generally required to gradually raise the temperature of the standby pressure reducing system even if the original temperature is lower so as to prevent the sudden heat shock of receiving high-pressure oil to damage the pressure reducer or other parts, in the conventional method, a high-temperature and basically solid hydrocarbon liquid material existing in a way of factory is introduced, but the temperature of the material (generally 250-350 ℃) is generally far lower than the normal operating temperature (generally 400-430 ℃) of the high-pressure oil, so that the ideal preheating effect cannot be realized, and the temperature of the normal preheating oil is difficult to flexibly adjust (limited by the process operating temperature at the source of the preheating oil), so that the high-pressure oil reducing system always has the problem that the preheating effect is not ideal.
In order to solve the foregoing problems, the present invention proposes a method of using flushing oil, the basic idea of which is: a method for flushing a main hot high-pressure oil reducer containing solid products in the hydrogenation process of hydrocarbon materials includes such steps as using flushing oil WS which is 5-20% of normal flow of hot high-pressure oil and is basically free of solid to establish soft lower limit basic flow R1 of main hot high-pressure oil reducer KV, running before coal is fed into a direct coal liquefaction reaction system R10, running after coal is fed into the system R10 normally or is stopped, when the THPSE liquid level of a hot high-pressure separator is too low and the emergency limit of KV is required to prevent the THPSE from continuously discharging liquid outwards, the lower limit position of KV opening is not zero flow and is fully closed, but a certain flow value is as small as 0.5R1-0.6R1, at this time, WS is divided into two paths, one path flows reversely and pushes hot high-pressure oil to return to the hot high-pressure separator, one path flows forward to flush solid at the sealing surface position of KV valve seat and valve core, and after the flushing process is continued for a period of time, the KV and a downstream liquid level control valve is closed again, so that the service life of the valve can be prolonged.
The flushing oil can be added from a flow point upstream of the main pressure reducer KV of the thermal macromolecule oil and passes through upstream pipeline equipment such as a pre-pressure reducing valve (such as an auxiliary pressure reducing valve) and a switching valve (such as a ball valve) for controlling the state of a pipeline flow path.
In order to ensure that the temperature of the flushing oil WS is proper (the temperature difference of the flushing oil WS and a system to be flushed is as close as possible), the temperature of the flushing oil WS can be raised through a heat exchanger or a heating furnace before the flushing oil WS enters the main hot oil-separating pressure reducer, and a pressurizing pump of the flushing oil WS is preferably positioned at a flow point with lower temperature, namely the flushing oil WS is pressurized and then raised so as to reduce the operation temperature of the booster pump, reduce the manufacturing cost and improve the running period.
The pressure-increasing and temperature-increasing system of the flushing oil WS can be simultaneously used as a high-temperature flushing oil system of the hydrogenation system R10, the constant-temperature flushing oil XTWS with various different temperature values can be prepared by adjusting the relative flow ratio of the high-temperature flushing oil TWS after temperature increasing and the flushing oil CWS before temperature increasing, flushing fluid with proper temperature can be provided for a plurality of flushing points with different operating temperatures, and flushing fluid with proper temperature and proper pressure can be provided for a plurality of flushing points with different operating temperatures and operating pressures by arranging the pressure reducer.
The invention can eliminate the severe erosion of solid particles on the sealing surface of the valve in the opening and closing process of the valve and the extrusion damage of the solid particles on the sealing surface in the seat returning process of the valve, prolongs the service life of the sealing surface of the valve, and is beneficial to improving the concentration of the solid particles in the hot high-pressure oil.
The working principle of the invention is to maintain a low limit solid-free liquid flow, and the source of the basic flow liquid of the flushing oil WS is at least:
(1) solid-free hydrocarbon oil from outside the coal hydrogenation direct liquefaction device;
(2) fractionating the hot high-fraction oil to obtain a solids-free distillate;
(3) hydrocarbon oil which may be condensate of hot high-pressure gas from the hot high-pressure separator THPSE;
(4) no components with a conventional boiling point below 250 ℃ or no components with a conventional boiling point below 280 ℃ are included to reduce cavitation.
The working principle of the invention is to maintain a low limit solid-free liquid flow, and the working time period of the flushing oil WS is as follows:
(1) the initial start-up process of the coal hydrogenation direct liquefaction device;
(2) the middle operation process of the coal hydrogenation direct liquefaction device;
(3) an emergency interlocking cutting-off process of the coal hydrogenation direct liquefaction device;
(4) a shutdown process of the coal hydrogenation direct liquefaction device;
(5) a heating and flushing process of a standby pressure reducing valve of the coal hydrogenation direct liquefaction device;
(6) the temperature-reducing flushing process of the pressure-reducing valve for the coal hydrogenation direct liquefying device from the working state to the standby state.
Other similar methods have not been reported so far.
The first aim of the invention is to provide a flushing method of a main hot high-pressure oil-separating pressure reducer containing solid products in the hydrogenation process of hydrocarbon materials.
The second aim of the invention is to provide a soft start-stop mode of the main pressure reducer of the hot high-pressure oil containing solid products in the hydrogenation process of the hydrocarbon material.
Disclosure of Invention
The invention relates to a flushing method of a main hot high-pressure oil-separating pressure reducer containing solid products in a hydrocarbon material hydrogenation process, which is characterized by comprising the following steps of:
in a first hydrogenation reaction process R10, a first hydrogenation reaction R10R is carried out on a hydrocarbon raw material R10F under the existence of hydrogen and a first hydrogenation catalyst R10C possibly existing to obtain a first hydrogenation reaction effluent R10P containing hydrogen, low-boiling-point hydrocarbon, high-boiling-point hydrocarbon and solids;
the first hydrogenation reaction process R10 has the functions of hydrogenation and/or hydro-thermal cracking on at least one part of hydrocarbon raw material R10F;
the first hydrogenation catalyst R10C which may be present generally has the functions of hydrogenation and or hydrogenation thermal cracking;
the first hydrogenation reaction R10R comprises at least a portion of a hydrofinishing reaction and/or at least a portion of a hydro thermal cracking reaction;
in the process of thermal high-pressure separation of the HTPS, the first hydrogenation reaction effluent R10P is subjected to gas-liquid separation to obtain solid-containing thermal high-pressure oil HTPS-L and thermal high-pressure gas HTPS-V; a hot high pressure separation process HTPS, possibly using gaseous hydrogen HTPS-HG, in contact with the liquid material from the first hydrogenation reaction effluent R10P to remove at least a portion of the low boiling components in the liquid phase;
At least a portion of the hot high-split oil HTPS-L or the de-aerated oil thereof is used as an erosion material into the hot high-split oil depressurization system DP;
thirdly, in the hot high-pressure oil-separating depressurization system DP, a main depressurization device KV with at least depressurization function is used, the main depressurization device KV bears most of pressure difference in the hot high-pressure oil-separating depressurization process in normal operation, a hot high-pressure separator THPSE is used for regulating the liquid level of the main depressurization device KV, and a flushing system is arranged;
in a depressurization system DP of a hot high-pressure oil HTPS-L, using a low-solid-content flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
the low-solid-content flushing oil WS refers to that the solid weight content in the flushing oil WS is lower than that in the hot high-fraction oil;
the soft lower limit basic flow R1 is smaller than the hot high-pressure oil HTPS-L flow;
when the liquid level of the hot high-pressure separator THPSE is too low and the main pressure reducer KV is required to reduce the opening degree, the lower limit position of the opening degree of the KV is not a zero flow fully-closed valve position, but is a small opening degree corresponding to a flow value which is smaller than R1 and is not zero, at the moment, WS is divided into two paths, one path of WS reversely flows and pushes hot high-pressure oil to return to the hot high-pressure separator THPSE, one path of WS forward flows to flush solids in an internal flow channel and a wall of the KV, and after the flushing process lasts for a period of time, the KV or an upstream valve with a closing function is closed, so that the service life of the main pressure reducer KV is prolonged;
The flushing oil WS is hydrocarbon oil discharged from the booster pump, and in order to ensure that the temperature of the flushing oil WS is proper, i.e. the temperature difference between the flushing oil WS and a system to be flushed is as close as possible, the temperature of the flushing oil WS is raised through a heat exchanger or a heating furnace before the flushing oil WS enters a main hot-oil-separating pressure reducer, i.e. the booster pump of the flushing oil WS is positioned at a flow point with lower temperature, i.e. the flushing oil WS is pressurized first and then raised to reduce the operation temperature of the booster pump.
According to the invention, the flushing system is arranged in the hot high-pressure oil-separating depressurization system DP, and the working mode of the flushing system can be selected from one or more of the following modes:
(1) in a depressurization system DP of a hot high-pressure oil HTPS-L, using a solid-free flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
(2) before the first hydrogenation reaction effluent R10P contains solids, firstly using a solid-free flushing oil WS to enter a feeding system of a main pressure reducer KV to establish a soft lower limit basic flow R1 of a hot high-pressure oil-separating pressure reducing system DP;
(3) in the normal production operation process after the first hydrogenation reaction effluent R10P contains solids, the solid-free flushing oil WS continuously enters a feeding system of the main pressure reducer KV and keeps the injection state;
(4) in the shutdown process from the reduction of the solid concentration in the first hydrogenation effluent R10P of the first hydrogenation process R10 until no solid is contained, continuously entering a feeding system of a main pressure reducer KV by using the solid-free flushing oil WS, and keeping the injection state;
(5) In the first hydrogenation reaction process R10, the solid concentration in the first hydrogenation reaction effluent R10P is reduced until the reaction system without solid is flushed, and the solid-free flushing oil WS continuously enters a feeding system of a main pressure reducer KV and is kept in a normal injection state;
(6) when the liquid level of the hot high-pressure separator THPSE is too low and the main pressure reducer KV is required to reduce the opening degree, the lower limit position of the opening degree of the KV is not a zero flow full-closed valve position, but is a small opening degree corresponding to a flow value which is smaller than R1 and is not zero, at the moment, WS is divided into two paths, one path of WS reversely flows and pushes hot high-pressure oil to return to the hot high-pressure separator THPSE, one path of WS forward flows to flush solids on the inner flow channel and the wall of the KV, and after the flushing process is continued for a period of time, the KV or an upstream valve with a closing function is closed, so that the service life of the main pressure reducer KV is prolonged.
In the invention, the source of the flushing oil WS can be selected from one or more of the following:
(1) solid-free hydrocarbon oil from outside the coal hydrogenation direct liquefaction device;
(2) fractionating the hot high-fraction oil to obtain a solids-free distillate;
(3) hydrocarbon oil from condensate of hot high-pressure gas of the hot high-pressure separator THPSE;
(4) no components with conventional boiling points lower than 280 ℃.
The invention provides a flushing oil system of flushing oil WS, which can be used as a high-temperature flushing oil system at the same time, and a plurality of constant-temperature flushing oil XTWS with different temperature values are prepared by preparing the relative flow ratio of the high-temperature flushing oil TWS after temperature rise and the flushing oil CWS before temperature rise, so that flushing fluid with proper temperature is provided for a plurality of flushing points with different operating temperatures.
In the present invention, the flushing oil WS may be hydrocarbon oil discharged from a reciprocating pump using a variable frequency governor.
According to the invention, the first hydrogenation reaction process R10 may be selected from 1 or several of the following processes:
(1) the coal hydrogenation direct liquefaction reaction process;
(2) heavy oil hydrogenation thermal cracking reaction process.
In the present invention, the first hydrogenation reaction process R10 may be selected from one or more of the following hydrogenation reaction processes:
(1) the coal hydrogenation direct liquefaction oil production process comprises an oil-coal co-refining process and a coal hydro-thermal liquefaction process;
(2) the hydrogenation process of the oil product obtained by using the upflow expansion bed in the middle and low temperature coal tar or the distillate oil thereof or the thermal processing process thereof, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(3) the hydrogenation process of the high-temperature coal tar or the distillate oil thereof or the oil product obtained in the hot working process thereof by using the upflow expansion bed, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(4) the hydrogenation process of the oil product obtained by shale oil or distillate oil thereof or a thermal processing process thereof by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(5) A hydrogenation process of ethylene pyrolysis tar using an upflow expanded bed;
(6) the hydrogenation process of the oil product obtained in the petroleum-based heavy oil thermal processing process by using the upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(7) the hydrogenation process of the oil product obtained in the petroleum sand-based heavy oil thermal processing process by using the upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(8) hydrogenation process of hydrocarbon oils with other aromatics weight content higher than 40% and organic nitrogen weight content higher than 0.10% using an upflow expanded bed.
In the invention, the hydrocarbon raw material R10F can be selected from one or more of the following materials:
(1) the low-temperature coal tar or distillate oil thereof or oil products obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a hydrogenation process;
(2) medium-temperature coal tar or distillate oil thereof or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(3) The high-temperature coal tar or distillate oil thereof or oil products obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(4) the coal liquefied oil or the distillate oil thereof obtained in the coal liquefied process or the oil obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process; the coal liquefaction process is selected from the processes of directly liquefying coal by using hydrogen-supplying solvent oil, oil-coal co-refining, and hydrothermally liquefying coal;
(5) shale oil or distillate oil thereof or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(6) ethylene cracking tar or oil products obtained in the thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(7) thermal cracking tar in petroleum-based wax oil;
(8) dan Yousha base oil or distillate oil thereof or oil obtained by a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(9) Petroleum-based heavy oil or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
and (b) other hydrocarbon oils having an aromatic hydrocarbon content of greater than 40% by weight and an organic nitrogen content of greater than 0.10% by weight.
In the present invention, the operating conditions are typically:
the method comprises the following steps that in a first hydrogenation reaction process R10, the operating pressure is 4.0-40 MPa, the operating temperature is 300-480 ℃, and the weight of solids in a first hydrogenation reaction effluent R10P accounts for 5-40% of the weight of solids plus the weight of conventional liquid hydrocarbon;
the operating pressure PB of the outlet of the main pressure reducer KV is 2-70% of the operating pressure PA of the Yu Regao pressure separation process.
In the invention, the operating conditions can be as follows:
the operating pressure PB of the outlet of the main pressure reducer KV used by the hot high-pressure oil-separating pressure reducing system DP is 5% -60% of the operating pressure PA of the hot high-pressure separation process.
In the invention, the operating conditions can be as follows:
the operating pressure PB of the outlet of the main pressure reducer KV used by the hot high-pressure oil-separating pressure reducing system DP is 10% -25% of the operating pressure PA of the hot high-pressure separation process.
In the present invention, the operating conditions are typically:
Setting a flushing system in the hot high-pressure oil distribution depressurization system DP;
in a depressurization system DP of a hot high-pressure oil HTPS-L, using a solid-free flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
the soft lower limit basic flow R1 is 5-20% of the weight flow of the hot high-pressure oil HTPS-L.
Drawings
Fig. 1 is a schematic flow chart of a principle of a flushing method of a main pressure reducer for hot high-pressure oil containing solid products in a hydrocarbon hydrogenation process, which comprises a hot high-pressure separator THPSE for directly liquefying a reaction product R10P from coal hydrogenation, a hot high-pressure oil emergency cut-off self-protection valve FSV, a liquid level regulating valve KV (main pressure reducer KV) of the hot high-pressure separator, a hot low-pressure separation part TLPS and a hot low-pressure oil separation part FRAC1.
As shown in fig. 1, the coal hydrogenation direct liquefaction reaction product R10P enters a hot high pressure separator THPSE through a pipeline 151 and is separated into hot high-pressure gas THPS-V conveyed along the pipeline 153 and hot high-pressure oil THPS-L conveyed along a pipeline 155, and the hot high-pressure oil THPS-L flows into a main pressure reducer KV through a pipeline 157 after passing through an emergency cut-off self-protection valve FSV; the flushing oil WS is conveyed by a pipeline 201 and is mixed with hot high-pressure oil THPS-L in a pipeline 157 to be fed FSV-F of a main pressure reducer KV, the fed KV-F flows through the main pressure reducer KV and is conveyed along a pipeline 158 to be fed as a low-pressure separator TLPS-F, and the fed TLPS-F enters a hot low-pressure separation part TLPS through the pipeline 158 to be separated into hot low-pressure gas TLPS-V conveyed along a pipeline 163 and hot low-pressure oil TLPS-L conveyed along a pipeline 165; the hot low-fraction oil TLPS-L enters the hot low-fraction oil fractionation section FRAC1 via a line 165, and is separated or fractionated to obtain a narrow fraction oil, and FIG. 1 shows a narrow fraction oil XP01 (e.g., a fraction oil having a conventional boiling point of less than 200 ℃) conveyed along a line 171, a narrow fraction oil XP02 (e.g., a fraction oil having a conventional boiling point of 200-330 ℃) conveyed along a line 172, a narrow fraction oil XP03 (e.g., a fraction oil having a conventional boiling point of 330-530 ℃) conveyed along a line 173, a narrow fraction oil XP04 (e.g., a residue having a conventional boiling point of greater than 530 ℃) conveyed along a line 174, and the like.
As shown in fig. 1, the source of the rinse oil WS is at least:
(1) the solid-free distillate oil conveyed along the pipeline 201 from the outside of the coal hydrogenation direct liquefaction device can be used for the initial start-up process and the shutdown process of the coal hydrogenation direct liquefaction device; the method can be used for the middle operation process and the emergency interlocking cutting-off process of the coal hydrogenation direct liquefaction device;
(2) the solid-free distillate oil obtained by fractionating the hot high-fraction oil can be used for the intermediate operation process, the emergency interlocking cutting-off process and the shutdown process of a coal hydrogenation direct liquefaction device.
As shown in fig. 1, the flushing oil WS0 may be introduced into the pipe 156 via the pipe 203, mixed with the hot high-fraction oil THPS-L from the pipe 155, passed through the emergency shut-off self-protection valve FSV, and then flowed into the main pressure reducer KV via the pipe 157, so that the flushing oil may simultaneously flush the emergency shut-off self-protection valve FSV, the main pressure reducer KV, and other pipe devices downstream.
Detailed Description
The pressure in the present invention refers to absolute pressure.
The conventional boiling point refers to the vapor-liquid equilibrium temperature of a substance at one atmosphere.
The conventional boiling range as used herein refers to the conventional boiling range of the distillate fraction.
The specific gravity according to the present invention means, unless otherwise specified, the ratio of the density of the liquid at normal pressure and 15.6 ℃ to the density of the water at normal pressure and 15.6 ℃.
The conventional gas hydrocarbon refers to hydrocarbon which is in a gaseous state under the conventional condition, and comprises methane, ethane, propane and butane.
The conventional liquid hydrocarbon used in the present invention refers to hydrocarbons which are liquid under conventional conditions, and includes pentane and hydrocarbons with higher boiling points.
The impurity elements described in the present invention refer to non-hydrogen, non-carbon, non-metal components such as oxygen, sulfur, nitrogen, chlorine, etc. in the raw oil.
The impurity component refers to hydroconversion of non-hydrocarbon components in the raw oil, such as water, ammonia, hydrogen sulfide, hydrogen chloride, and the like.
The middle distillate referred to herein refers to a hydrocarbon fraction suitable for use as diesel and/or naphtha, which may be naphtha and/or diesel.
The middle distillate component of the present invention refers to a hydrocarbon component suitable for use as diesel and or naphtha.
The naphtha component as described herein refers to a conventional liquid hydrocarbon component having a conventional boiling point generally below 220 c, generally below 190 c, and particularly 165 c.
The diesel fuel component according to the invention is a conventional liquid hydrocarbon having a conventional boiling point generally in the range 165 to 380 ℃, generally in the range 190 to 350 ℃, in particular in the range 220 to 330 ℃.
The heavy oil component of the present invention refers to conventional liquid hydrocarbons having conventional boiling points generally above 300 ℃, generally above 330 ℃, and particularly above 370 ℃. The heavy oil of the present invention may contain a part of middle distillate.
The pressure reducing valve is installed in any proper mode, the installation mode of the pressure reducer is vertical, the lower space of the pressure reducer split-phase bag is a liquid phase region, and the upper part of the pressure reducer is a gas phase region; at least most of liquid in the deceleration phase-splitting bag is discharged through a liquid flow discharge port, at least most of gas in the deceleration phase-splitting bag is discharged through a gas discharge port pipeline, jet flow discharged by a pressure reducing valve is sprayed to a liquid phase collecting area from the upper part of a liquid phase space, most of liquid and solid in the jet flow are injected into the liquid phase to form liquid phase waves, the high-speed jet flow is absorbed by the liquid to form low-speed dispersion flow, the liquid at the front end of an axis of the jet flow impact direction is reflected by a wall surface to form a region with zero flow velocity, static pressure is large in the region, the liquid deceleration process forms a static pressure field with static pressure rising rapidly, and the static pressure field provides resistance that most of jet flow reduces the impact velocity and can push the liquid to move around to form waves, vortexes and the like.
The characteristic parts of the present invention are described below.
The invention relates to a flushing method of a main hot high-pressure oil-separating pressure reducer containing solid products in a hydrocarbon material hydrogenation process, which is characterized by comprising the following steps of:
in a first hydrogenation reaction process R10, a first hydrogenation reaction R10R is carried out on a hydrocarbon raw material R10F under the existence of hydrogen and a first hydrogenation catalyst R10C possibly existing to obtain a first hydrogenation reaction effluent R10P containing hydrogen, low-boiling-point hydrocarbon, high-boiling-point hydrocarbon and solids;
The first hydrogenation reaction process R10 has the functions of hydrogenation and/or hydro-thermal cracking on at least one part of hydrocarbon raw material R10F;
the first hydrogenation catalyst R10C which may be present generally has the functions of hydrogenation and or hydrogenation thermal cracking;
the first hydrogenation reaction R10R comprises at least a portion of a hydrofinishing reaction and/or at least a portion of a hydro thermal cracking reaction;
in the process of thermal high-pressure separation of the HTPS, the first hydrogenation reaction effluent R10P is subjected to gas-liquid separation to obtain solid-containing thermal high-pressure oil HTPS-L and thermal high-pressure gas HTPS-V; a hot high pressure separation process HTPS, possibly using gaseous hydrogen HTPS-HG, in contact with the liquid material from the first hydrogenation reaction effluent R10P to remove at least a portion of the low boiling components in the liquid phase;
at least a portion of the hot high-split oil HTPS-L or the de-aerated oil thereof is used as an erosion material into the hot high-split oil depressurization system DP;
thirdly, in the hot high-pressure oil-separating depressurization system DP, a main depressurization device KV with at least depressurization function is used, the main depressurization device KV bears most of pressure difference in the hot high-pressure oil-separating depressurization process in normal operation, a hot high-pressure separator THPSE is used for regulating the liquid level of the main depressurization device KV, and a flushing system is arranged;
in a depressurization system DP of a hot high-pressure oil HTPS-L, using a low-solid-content flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
The low-solid-content flushing oil WS refers to that the solid weight content in the flushing oil WS is lower than that in the hot high-fraction oil;
the soft lower limit basic flow R1 is smaller than the hot high-pressure oil HTPS-L flow;
when the liquid level of the hot high-pressure separator THPSE is too low and the main pressure reducer KV is required to reduce the opening degree, the lower limit position of the opening degree of the KV is not a zero flow fully-closed valve position, but is a small opening degree corresponding to a flow value which is smaller than R1 and is not zero, at the moment, WS is divided into two paths, one path of WS reversely flows and pushes hot high-pressure oil to return to the hot high-pressure separator THPSE, one path of WS forward flows to flush solids in an internal flow channel and a wall of the KV, and after the flushing process lasts for a period of time, the KV or an upstream valve with a closing function is closed, so that the service life of the main pressure reducer KV is prolonged;
the flushing oil WS is hydrocarbon oil discharged from the booster pump, and in order to ensure that the temperature of the flushing oil WS is proper, i.e. the temperature difference between the flushing oil WS and a system to be flushed is as close as possible, the temperature of the flushing oil WS is raised through a heat exchanger or a heating furnace before the flushing oil WS enters a main hot-oil-separating pressure reducer, i.e. the booster pump of the flushing oil WS is positioned at a flow point with lower temperature, i.e. the flushing oil WS is pressurized first and then raised to reduce the operation temperature of the booster pump.
According to the invention, the flushing system is arranged in the hot high-pressure oil-separating depressurization system DP, and the working mode of the flushing system can be selected from one or more of the following modes:
(1) In a depressurization system DP of a hot high-pressure oil HTPS-L, using a solid-free flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
(2) before the first hydrogenation reaction effluent R10P contains solids, firstly using a solid-free flushing oil WS to enter a feeding system of a main pressure reducer KV to establish a soft lower limit basic flow R1 of a hot high-pressure oil-separating pressure reducing system DP;
(3) in the normal production operation process after the first hydrogenation reaction effluent R10P contains solids, the solid-free flushing oil WS continuously enters a feeding system of the main pressure reducer KV and keeps the injection state;
(4) in the shutdown process from the reduction of the solid concentration in the first hydrogenation effluent R10P of the first hydrogenation process R10 until no solid is contained, continuously entering a feeding system of a main pressure reducer KV by using the solid-free flushing oil WS, and keeping the injection state;
(5) in the first hydrogenation reaction process R10, the solid concentration in the first hydrogenation reaction effluent R10P is reduced until the reaction system without solid is flushed, and the solid-free flushing oil WS continuously enters a feeding system of a main pressure reducer KV and is kept in a normal injection state;
(6) when the liquid level of the hot high-pressure separator THPSE is too low and the main pressure reducer KV is required to reduce the opening degree, the lower limit position of the opening degree of the KV is not a zero flow full-closed valve position, but is a small opening degree corresponding to a flow value which is smaller than R1 and is not zero, at the moment, WS is divided into two paths, one path of WS reversely flows and pushes hot high-pressure oil to return to the hot high-pressure separator THPSE, one path of WS forward flows to flush solids on the inner flow channel and the wall of the KV, and after the flushing process is continued for a period of time, the KV or an upstream valve with a closing function is closed, so that the service life of the main pressure reducer KV is prolonged.
In the invention, the source of the flushing oil WS can be selected from one or more of the following:
(1) solid-free hydrocarbon oil from outside the coal hydrogenation direct liquefaction device;
(2) fractionating the hot high-fraction oil to obtain a solids-free distillate;
(3) hydrocarbon oil from condensate of hot high-pressure gas of the hot high-pressure separator THPSE;
(4) no components with conventional boiling points lower than 280 ℃.
The invention provides a flushing oil system of flushing oil WS, which can be used as a high-temperature flushing oil system at the same time, and a plurality of constant-temperature flushing oil XTWS with different temperature values are prepared by preparing the relative flow ratio of the high-temperature flushing oil TWS after temperature rise and the flushing oil CWS before temperature rise, so that flushing fluid with proper temperature is provided for a plurality of flushing points with different operating temperatures.
In the present invention, the flushing oil WS may be hydrocarbon oil discharged from a reciprocating pump using a variable frequency governor.
According to the invention, the first hydrogenation reaction process R10 may be selected from 1 or several of the following processes:
(1) the coal hydrogenation direct liquefaction reaction process;
(2) heavy oil hydrogenation thermal cracking reaction process.
In the present invention, the first hydrogenation reaction process R10 may be selected from one or more of the following hydrogenation reaction processes:
(1) the coal hydrogenation direct liquefaction oil production process comprises an oil-coal co-refining process and a coal hydro-thermal liquefaction process;
(2) The hydrogenation process of the oil product obtained by using the upflow expansion bed in the middle and low temperature coal tar or the distillate oil thereof or the thermal processing process thereof, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(3) the hydrogenation process of the high-temperature coal tar or the distillate oil thereof or the oil product obtained in the hot working process thereof by using the upflow expansion bed, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(4) the hydrogenation process of the oil product obtained by shale oil or distillate oil thereof or a thermal processing process thereof by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(5) a hydrogenation process of ethylene pyrolysis tar using an upflow expanded bed;
(6) the hydrogenation process of the oil product obtained in the petroleum-based heavy oil thermal processing process by using the upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(7) the hydrogenation process of the oil product obtained in the petroleum sand-based heavy oil thermal processing process by using the upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(8) Hydrogenation process of hydrocarbon oils with other aromatics weight content higher than 40% and organic nitrogen weight content higher than 0.10% using an upflow expanded bed.
In the invention, the hydrocarbon raw material R10F can be selected from one or more of the following materials:
(1) the low-temperature coal tar or distillate oil thereof or oil products obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a hydrogenation process;
(2) medium-temperature coal tar or distillate oil thereof or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(3) the high-temperature coal tar or distillate oil thereof or oil products obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(4) the coal liquefied oil or the distillate oil thereof obtained in the coal liquefied process or the oil obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process; the coal liquefaction process is selected from the processes of directly liquefying coal by using hydrogen-supplying solvent oil, oil-coal co-refining, and hydrothermally liquefying coal;
(5) Shale oil or distillate oil thereof or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(6) ethylene cracking tar or oil products obtained in the thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(7) thermal cracking tar in petroleum-based wax oil;
(8) dan Yousha base oil or distillate oil thereof or oil obtained by a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(9) petroleum-based heavy oil or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
and (b) other hydrocarbon oils having an aromatic hydrocarbon content of greater than 40% by weight and an organic nitrogen content of greater than 0.10% by weight.
In the present invention, the operating conditions are typically:
the method comprises the following steps that in a first hydrogenation reaction process R10, the operating pressure is 4.0-40 MPa, the operating temperature is 300-480 ℃, and the weight of solids in a first hydrogenation reaction effluent R10P accounts for 5-40% of the weight of solids plus the weight of conventional liquid hydrocarbon;
The operating pressure PB of the outlet of the main pressure reducer KV is 2-70% of the operating pressure PA of the Yu Regao pressure separation process.
In the invention, the operating conditions can be as follows:
the operating pressure PB of the outlet of the main pressure reducer KV used by the hot high-pressure oil-separating pressure reducing system DP is 5% -60% of the operating pressure PA of the hot high-pressure separation process.
In the invention, the operating conditions can be as follows:
the operating pressure PB of the outlet of the main pressure reducer KV used by the hot high-pressure oil-separating pressure reducing system DP is 10% -25% of the operating pressure PA of the hot high-pressure separation process.
In the present invention, the operating conditions are typically:
setting a flushing system in the hot high-pressure oil distribution depressurization system DP;
in a depressurization system DP of a hot high-pressure oil HTPS-L, using a solid-free flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
the soft lower limit basic flow R1 is 5-20% of the weight flow of the hot high-pressure oil HTPS-L.
Claims (12)
1. The method for flushing the main hot high-pressure oil separator containing solid products in the hydrocarbon material hydrogenation process is characterized by comprising the following steps of:
in a first hydrogenation reaction process R10, a first hydrogenation reaction R10R is carried out on a hydrocarbon raw material R10F under the existence of hydrogen and a first hydrogenation catalyst R10C possibly existing to obtain a first hydrogenation reaction effluent R10P containing hydrogen, low-boiling-point hydrocarbon, high-boiling-point hydrocarbon and solids;
The first hydrogenation reaction process R10 has the functions of hydrogenation and/or hydro-thermal cracking on at least one part of hydrocarbon raw material R10F;
the first hydrogenation catalyst R10C which may be present generally has the functions of hydrogenation and or hydrogenation thermal cracking;
the first hydrogenation reaction R10R comprises at least a portion of a hydrofinishing reaction and/or at least a portion of a hydro thermal cracking reaction;
in the process of thermal high-pressure separation of the HTPS, the first hydrogenation reaction effluent R10P is subjected to gas-liquid separation to obtain solid-containing thermal high-pressure oil HTPS-L and thermal high-pressure gas HTPS-V; a hot high pressure separation process HTPS, possibly using gaseous hydrogen HTPS-HG, in contact with the liquid material from the first hydrogenation reaction effluent R10P to remove at least a portion of the low boiling components in the liquid phase;
at least a portion of the hot high-split oil HTPS-L or the de-aerated oil thereof is used as an erosion material into the hot high-split oil depressurization system DP;
thirdly, in the hot high-pressure oil-separating depressurization system DP, a main depressurization device KV with at least depressurization function is used, the main depressurization device KV bears most of pressure difference in the hot high-pressure oil-separating depressurization process in normal operation, a hot high-pressure separator THPSE is used for regulating the liquid level of the main depressurization device KV, and a flushing system is arranged;
in a depressurization system DP of a hot high-pressure oil HTPS-L, using a low-solid-content flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
The low-solid-content flushing oil WS refers to that the solid weight content in the flushing oil WS is lower than that in the hot high-fraction oil;
the soft lower limit basic flow R1 is smaller than the hot high-pressure oil HTPS-L flow;
when the liquid level of the hot high-pressure separator THPSE is too low and the main pressure reducer KV is required to reduce the opening degree, the lower limit position of the opening degree of the KV is not a zero flow fully-closed valve position, but is a small opening degree corresponding to a flow value which is smaller than R1 and is not zero, at the moment, WS is divided into two paths, one path of WS reversely flows and pushes hot high-pressure oil to return to the hot high-pressure separator THPSE, one path of WS forward flows to flush solids in an internal flow channel and a wall of the KV, and after the flushing process lasts for a period of time, the KV or an upstream valve with a closing function is closed, so that the service life of the main pressure reducer KV is prolonged;
the flushing oil WS is hydrocarbon oil discharged from the booster pump, and in order to ensure that the temperature of the flushing oil WS is proper, i.e. the temperature difference between the flushing oil WS and a system to be flushed is as close as possible, the temperature of the flushing oil WS is raised through a heat exchanger or a heating furnace before the flushing oil WS enters a main hot-oil-separating pressure reducer, i.e. the booster pump of the flushing oil WS is positioned at a flow point with lower temperature, i.e. the flushing oil WS is pressurized first and then raised to reduce the operation temperature of the booster pump.
2. The method according to claim 1, wherein:
Third, in the hot high-pressure oil distribution depressurization system DP, a flushing system is provided, and the working mode of the flushing system is one or more of the following modes:
(1) in a depressurization system DP of a hot high-pressure oil HTPS-L, using a solid-free flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
(2) before the first hydrogenation reaction effluent R10P contains solids, firstly using a solid-free flushing oil WS to enter a feeding system of a main pressure reducer KV to establish a soft lower limit basic flow R1 of a hot high-pressure oil-separating pressure reducing system DP;
(3) in the normal production operation process after the first hydrogenation reaction effluent R10P contains solids, the solid-free flushing oil WS continuously enters a feeding system of the main pressure reducer KV and keeps the injection state;
(4) in the shutdown process from the reduction of the solid concentration in the first hydrogenation effluent R10P of the first hydrogenation process R10 until no solid is contained, continuously entering a feeding system of a main pressure reducer KV by using the solid-free flushing oil WS, and keeping the injection state;
(5) in the first hydrogenation reaction process R10, the solid concentration in the first hydrogenation reaction effluent R10P is reduced until the reaction system without solid is flushed, and the solid-free flushing oil WS continuously enters a feeding system of a main pressure reducer KV and is kept in a normal injection state;
(6) When the liquid level of the hot high-pressure separator THPSE is too low and the main pressure reducer KV is required to reduce the opening degree, the lower limit position of the opening degree of the KV is not a zero flow full-closed valve position, but is a small opening degree corresponding to a flow value which is smaller than R1 and is not zero, at the moment, WS is divided into two paths, one path of WS reversely flows and pushes hot high-pressure oil to return to the hot high-pressure separator THPSE, one path of WS forward flows to flush solids on the inner flow channel and the wall of the KV, and after the flushing process is continued for a period of time, the KV or an upstream valve with a closing function is closed, so that the service life of the main pressure reducer KV is prolonged.
3. The method according to claim 1, wherein:
the source of the flushing oil WS is selected from one or more of the following:
(1) solid-free hydrocarbon oil from outside the coal hydrogenation direct liquefaction device;
(2) fractionating the hot high-fraction oil to obtain a solids-free distillate;
(3) hydrocarbon oil from condensate of hot high-pressure gas of the hot high-pressure separator THPSE;
(4) no components with conventional boiling points lower than 280 ℃.
4. The method according to claim 1, wherein:
the flushing oil system of the flushing oil WS is provided, and meanwhile, the flushing oil system also serves as a high-temperature flushing oil system, and the constant-temperature flushing oil XTWS with various different temperature values is prepared by adjusting the relative flow ratio of the high-temperature flushing oil TWS after temperature rise and the flushing oil CWS before temperature rise, so that flushing fluid with proper temperature is provided for a plurality of flushing points with different operating temperatures.
5. The method according to claim 1, wherein:
the flushing oil WS is hydrocarbon oil discharged from a reciprocating pump using a variable frequency governor.
6. The method according to claim 1, wherein:
the first hydrogenation reaction process R10 is selected from 1 or more of the following processes:
(1) the coal hydrogenation direct liquefaction reaction process;
(2) heavy oil hydrogenation thermal cracking reaction process.
7. The method according to claim 1, wherein:
the first hydrogenation reaction process R10 is selected from one or more of the following hydrogenation reaction processes:
(1) the coal hydrogenation direct liquefaction oil production process comprises an oil-coal co-refining process and a coal hydro-thermal liquefaction process;
(2) the hydrogenation process of the oil product obtained by using the upflow expansion bed in the middle and low temperature coal tar or the distillate oil thereof or the thermal processing process thereof, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(3) the hydrogenation process of the high-temperature coal tar or the distillate oil thereof or the oil product obtained in the hot working process thereof by using the upflow expansion bed, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(4) the hydrogenation process of the oil product obtained by shale oil or distillate oil thereof or a thermal processing process thereof by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(5) A hydrogenation process of ethylene pyrolysis tar using an upflow expanded bed;
(6) the hydrogenation process of the oil product obtained in the petroleum-based heavy oil thermal processing process by using the upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(7) the hydrogenation process of the oil product obtained in the petroleum sand-based heavy oil thermal processing process by using the upflow expansion bed, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(8) hydrogenation process of hydrocarbon oils with other aromatics weight content higher than 40% and organic nitrogen weight content higher than 0.10% using an upflow expanded bed.
8. The method according to claim 1, wherein:
the hydrocarbon raw material R10F is selected from one or more of the following materials:
(1) the low-temperature coal tar or distillate oil thereof or oil products obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a hydrogenation process;
(2) medium-temperature coal tar or distillate oil thereof or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(3) The high-temperature coal tar or distillate oil thereof or oil products obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(4) the coal liquefied oil or the distillate oil thereof obtained in the coal liquefied process or the oil obtained in the hot working process, wherein the hot working process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process; the coal liquefaction process is selected from the processes of directly liquefying coal by using hydrogen-supplying solvent oil, oil-coal co-refining, and hydrothermally liquefying coal;
(5) shale oil or distillate oil thereof or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(6) ethylene cracking tar or oil products obtained in the thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(7) thermal cracking tar in petroleum-based wax oil;
(8) dan Yousha base oil or distillate oil thereof or oil obtained by a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
(9) Petroleum-based heavy oil or oil products obtained in a thermal processing process, wherein the thermal processing process is a heavy oil coking process or a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
and (b) other hydrocarbon oils having an aromatic hydrocarbon content of greater than 40% by weight and an organic nitrogen content of greater than 0.10% by weight.
9. The method according to claim 1, wherein:
the method comprises the following steps that in a first hydrogenation reaction process R10, the operating pressure is 4.0-40 MPa, the operating temperature is 300-480 ℃, and the weight of solids in a first hydrogenation reaction effluent R10P accounts for 5-40% of the weight of solids plus the weight of conventional liquid hydrocarbon;
the operating pressure PB of the outlet of the main pressure reducer KV is 2-70% of the operating pressure PA of the Yu Regao pressure separation process.
10. The method according to claim 9, wherein:
the operating pressure PB of the outlet of the main pressure reducer KV used by the hot high-pressure oil-separating pressure reducing system DP is 5% -60% of the operating pressure PA of the hot high-pressure separation process.
11. The method according to claim 9, wherein:
the operating pressure PB of the outlet of the main pressure reducer KV used by the hot high-pressure oil-separating pressure reducing system DP is 10% -25% of the operating pressure PA of the hot high-pressure separation process.
12. The method according to claim 1, wherein:
setting a flushing system in the hot high-pressure oil distribution depressurization system DP;
in a depressurization system DP of a hot high-pressure oil HTPS-L, using a solid-free flushing oil WS to enter a feeding system of a main depressurization device KV of the hot high-pressure oil HTPS-L, and establishing a soft lower limit basic flow R1 of the depressurization system DP of the hot high-pressure oil HTPS-L;
the soft lower limit basic flow R1 is 5-20% of the weight flow of the hot high-pressure oil HTPS-L.
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