CN108504379B - Soft start-stop method of hot high-oil-separation depressurization system containing solid hydrogenation products - Google Patents
Soft start-stop method of hot high-oil-separation depressurization system containing solid hydrogenation products Download PDFInfo
- Publication number
- CN108504379B CN108504379B CN201710149329.8A CN201710149329A CN108504379B CN 108504379 B CN108504379 B CN 108504379B CN 201710149329 A CN201710149329 A CN 201710149329A CN 108504379 B CN108504379 B CN 108504379B
- Authority
- CN
- China
- Prior art keywords
- oil
- hydrogenation
- hot high
- separation
- heavy oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- C—CHEMISTRY; METALLURGY
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A soft start-stop method of a hot high-oil separation depressurization system containing solid hydrogenation products is characterized in that solid-free flushing oil WS with the normal flow of hot high-oil separation of 5-20% is used for establishing the soft lower limit basic flow R1 of the hot high-oil separation depressurization system, the operation is carried out before the coal hydrogenation direct liquefaction reaction system R10 is put into operation, the operation is continued in the normal coal feeding process of R10 or after the coal feeding is stopped, when the liquid level of the hot high-pressure separator THPSE is too low and requires the hot high-pressure oil separation self-protection valve KV to be turned off in an emergency, the turn-off position of the KV is not the zero flow full-off in the conventional scheme, and a certain flow value is as small as 0.5R 1-0.6R 1, WS is divided into two paths, one path flows reversely and pushes hot high-pressure oil to return to the hot high-pressure separator, the other path flows forwards to wash the solid at the sealing surface position of the valve seat and the valve core of KV, and after the washing process lasts for a period of time, the KV and the downstream liquid level control valve are closed, so that the service life of the valve can be prolonged.
Description
Technical Field
The invention relates to a soft start-stop method of a hot high-oil separation depressurization system containing solid hydrogenation products, wherein solid-free flushing oil WS with the normal flow of 5-20% of the hot high-oil separation is used for establishing the soft lower limit basic flow R1 of the hot high-oil separation depressurization system, the operation is carried out before coal is put into a direct coal hydrogenation liquefaction reaction system R10, the operation is continued in the normal coal feeding process of R10 or after the coal is put into the system, when the THPSE liquid level of a hot high-pressure separator is too low and requires the emergency shut-off of a hot high-oil separation self-protection valve KV, the shut-off position of the KV is not the zero flow full shut-off in the conventional scheme, but is a small opening corresponding to a certain flow value such as 0.5R 1-0.6R 1, at the moment, the WS is divided into two paths, one path reversely flows and pushes the hot high-oil separation to return to the hot high-oil separation separator, the other path flows to flush the solid at the sealing surface position of the valve, the service life of the valve can be prolonged.
Background
The solid hydrogenation product of the present invention is solid particles, most of which are particles of pulverized coal, semicoke and catalyst, and generally have a particle size of less than 200 microns, generally less than 50 microns, preferably less than 10 microns.
The separation process of the coal hydrogenation direct liquefaction reaction product of Shenhua Ordos coal oil separation company in China is a hot high-pressure flash separation method, 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 material flow THPS-L and hot high-separation gas THPS-V containing most solid products, the liquid-solid mixed phase material flow THPS-L is called hot high-separation oil THPS-L for short, and the method is a custom name which is known by technical personnel in the field and is a solid-containing oil material. Generally, after the hot high-molecular oil THPS-L is subjected to 1-stage depressurization, 2-stage depressurization or multi-stage depressurization, the hot high-molecular oil THPS-L enters a distillation process FRAC1 to complete the separation of solid and hydrocarbon components to obtain distilled oil FRAC1-MH and residue mainly composed of solid and heavy hydrocarbon, and the distilled oil FRAC1-MH is generally processed by combining with the hydrocarbon components THPS-V-LM in the hot high-molecular gas THPS-V; the hot high-fraction oil THPS-L is extremely harsh in operation conditions for pressure reduction equipment, the operation pressure is 18-19 MPa, the operation pressure difference is 14-15 MPa, the operation temperature is 400-430 ℃, a large amount of hydrogen is dissolved in the hot high-fraction oil under high-pressure and high-temperature conditions, about 40-60% of medium-boiling-point hydrocarbons such as normal hydrocarbons with the boiling point of 250-350 ℃ exist in the hot high-fraction oil in a liquid state and contain 6-25% of solid particles, and the hot high-fraction oil enters a hot low-pressure separator TLPS after the pressure is reduced to 2.0-4.0 MPa through a pressure reducer and is separated into hot low-fraction gas TLPS-V and hot low-fraction oil TLPS-L; then the hot low-fraction oil TLPS-L is further depressurized and then subjected to a distillation process FRAC 1.
According to the thermal high-pressure flash evaporation separation method of the direct coal hydrogenation liquefaction reaction product, the thermal high-fraction oil THPS-L is a liquid-solid mixed phase material flow which is high in pressure and temperature, contains solids, corrosive components and a large amount of soluble gas and low-boiling-point hydrocarbon components, and the pressure reduction process of the thermal high-fraction oil THPS-L inevitably forms strong erosion on the pressure reduction valve flow passage component, so that the service life of the flow passage component is seriously shortened; meanwhile, in the sudden change process of the operation state of the hot high-pressure separator THPSE, such as the starting discharge process of starting to release solid-containing hot high-separation oil, the small-opening valve opened in a fully closed state is actually a flow-limiting orifice plate of a small flow channel, and liquid with high solid content can quickly erode the edge of the flow-limiting orifice plate of the small flow channel, namely a valve sealing surface, under the driving of high differential pressure; similarly, in the sudden change process of the operation state of the hot high-pressure separator THPSE, such as the emergency cut-off closing process of hot high-pressure oil separation, the small-opening valve which quickly reaches the closing state from the normal opening also is a flow-limiting orifice plate of a small flow passage, and the edge of the flow-limiting orifice plate of the small flow passage, namely the valve sealing surface, can be quickly eroded by the liquid with high solid content under the drive of high differential pressure; the more dangerous condition is, in the operation state sudden change process of hot high pressure separator THPSE such as hot high oil separator emergency cut-off closing process, reach the valve of closed condition rapidly by normal aperture, its case returns the seat to the sealed face of valve seat and forms the process of closed condition, can't guarantee that there is absolutely no solid particle between this closed pair of sealed faces, therefore there is extrusion damage to sealed face in fact certainly having solid particle, that is to say, the sealed face of valve is put into the buggy each time, the process of emergency cut-off closing each time, all formed the damage, shortened the sealed face life of valve, be unfavorable for prolonging device continuous operation cycle.
In order to inhibit the damage, the invention provides a soft opening and closing mode, and the basic idea is as follows: a soft start-stop method of a hot high oil separation depressurization system containing solid hydrogenation products comprises the steps of establishing a soft lower limit basic flow R1 circulation loop LP100 of the hot high oil separation depressurization system by using solid-free circulating flushing oil WS with the normal flow of 5-20%, running the system before coal is thrown into a coal hydrogenation direct liquefaction reaction system R10, running the LP100 continuously after the R10 normal coal feeding process or coal throwing stopping, when the THPSE liquid level of a hot high pressure separator is too low and requires the hot high oil separation self-maintaining valve KV to be turned off emergently, turning off the KV position instead of the zero flow full-off in the conventional scheme, but a certain flow value such as 0.5R 1-0.6R 1 corresponding small opening degree, at the moment, the WS is divided into two paths, one path flows reversely and pushes the hot high oil separation to return to the high pressure separator or go to other paths, one path flows forward to flush solids at the valve seat and valve core sealing surface position of the KV, and the downstream valve such as a liquid level control valve after the flushing process lasts for a period, the service life of the valve can be prolonged.
The invention can eliminate the violent erosion of the solid particles to the sealing surface of the valve in the opening and closing process of the valve and the extrusion damage of the solid particles to the sealing surface in the seat returning process of the valve, prolong the service life of the sealing surface of the valve and is beneficial to improving the concentration of the solid particles in high-temperature oil.
The working principle of the invention is to maintain a low-limit solid-free liquid flow, and the basic flow liquid of the invention at least has the following sources:
firstly, the solid-free hydrocarbon oil 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 intermediate operation process and the emergency interlocking cutting-off process of the direct coal hydrogenation liquefaction device;
the solid-free distillate oil obtained by fractionating the hot high-temperature separation oil can be used in the middle operation process, the emergency interlocking cutting-off process and the shutdown process of the coal hydrogenation direct liquefaction device;
and thirdly, the low-pressure degasification oil of the hot high-separation oil, namely the solid-containing hot low-separation oil or the solid-removing liquid of the cyclone separator thereof can be used for the intermediate operation process and the emergency interlocking cutting-off process of the direct coal hydrogenation liquefaction device.
So far, other methods of the same type have not been reported.
The invention aims to provide a soft start-stop method of a hot high-oil-separation depressurization system containing solid hydrogenation products.
The second purpose of the invention is to provide a soft opening and closing mode of a solid product-containing thermal high-pressure oil-separation depressurization system for poor-quality oil suspension bed hydrogenation reaction.
The third purpose of the invention is to provide a soft start-stop mode of the hot high-oil-separation depressurization system for the direct coal hydrogenation liquefaction product.
Disclosure of Invention
The invention discloses a soft start-stop method of a hot high-oil-separation depressurization system containing a solid hydrogenation product, which is characterized by comprising the following steps of:
(1) in a first hydrogenation process R10, a hydrocarbon feedstock R10F is subjected to a first hydrogenation reaction R10R in the presence of hydrogen and a first hydrogenation catalyst R10C, if present, to obtain a first hydrogenation reaction effluent R10P comprising hydrogen, low boiling hydrocarbons, high boiling hydrocarbons and solids;
the first hydrogenation reaction process R10 has the function of hydrogenation and/or hydrocracking at least a part of the hydrocarbon raw material R10F;
a first hydrogenation catalyst R10C, which may be present, overall having the function of hydrogenation and/or hydrocracking;
the first hydrogenation reaction R10R comprises at least a portion of a hydrofinishing reaction and/or at least a portion of a hydrothermally cracking reaction;
(2) in the HTPS process, the first hydrogenation reaction effluent R10P is subjected to gas-liquid separation to obtain solid-containing hot high-molecular oil HTPS-L and hot high-molecular gas HTPS-V; a hot high pressure separation process HTPS, possibly using gaseous hydrogen HTPS-HG to contact the liquid feed from the first hydrogenation effluent R10P to remove at least a portion of the low boiling components in the liquid phase;
at least one part of the hot high-oil separation HTPS-L or medium-pressure deaerated oil is used as an erosion material entering a hot high-oil separation depressurization system DP;
(3) in a hot high-oil separation depressurization system DP, a self-protection valve KV with an emergency cut-off function is used, a flow controller CV for regulating the liquid level of a hot high-pressure separator THPSE is used, and a soft start-stop system is arranged;
in a depressurization system DP of the hot high-oil separation HTPS-L, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and establishing a soft lower limit basic flow R1 of the hot high-oil separation depressurization system DP;
the basic flow R1 is smaller than the flow of the thermal high-oil separation HTPS-L;
when the liquid level of the hot high-pressure separator THPSE is too low and the self-protection valve KV of hot high-pressure oil separation is required to be turned off emergently, the turn-off position of the self-protection valve KV is not a zero-flow full-closed valve position, but is not zero and is smaller than a small opening degree corresponding to a flow value of R1, at the moment, the solid-free flushing oil WS is divided into two paths, one path of the solid-free flushing oil WS reversely flows and pushes the hot high-pressure oil separation to return to the hot high-pressure separator THPSE, the other path of the solid-free flushing oil WS flows in the forward direction to flush solids at the positions of a valve seat and a valve core sealing surface of the self-protection valve KV, and after the flushing.
The working mode of the invention is generally as follows:
(3) a soft opening and closing system is arranged in a hot high oil separation depressurization system DP;
in a depressurization system DP of the hot high-oil separation HTPS-L, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and establishing a soft lower limit basic flow R1 of the hot high-oil separation depressurization system DP;
before the first hydrogenation reaction effluent R10P contains solids, firstly, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV to establish a soft lower limit basic flow R1 of a hot high-oil-separation depressurization system DP;
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 an emergency cut-off self-protection valve KV and is kept injected to be in a normal state;
when the first hydrogenation reaction effluent R10P is reduced until the first hydrogenation reaction process R10 is shut down, the solid-free flushing oil WS continuously enters a feeding system of an emergency cut-off self-protection valve KV and is kept injected to be normal;
when the first hydrogenation reaction effluent R10P is reduced until the first hydrogenation reaction process R10 flushing process without solids is carried out, the solid-free flushing oil WS continuously enters a feeding system of an emergency cut-off self-protection valve KV and is kept injected to be in a normal state;
when the liquid level of the high-pressure hot separator THPSE is too low and the requirement for emergency shutdown of the high-pressure hot separator THPSE is met, the shutdown position of the self-protection valve KV is not a zero-flow full-closed valve position, but is not zero and smaller than a small opening corresponding to a flow value R1, at the moment, the solid-free flushing oil WS is divided into two paths, one path of the solid-free flushing oil WS reversely flows and pushes the high-pressure hot separator THPSE to return to the high-pressure hot separator THPSE, the other path of the solid-free flushing oil WS forwardly flows to flush solids at the positions of a valve seat and a valve core sealing surface of the self-protection valve KV, and after the flushing process lasts for a period of time, the self-protection valve KV and the liquid level control valve CV of the.
In the present invention, the flushing oil WS is generally hydrocarbon oil discharged from a reciprocating pump.
In the invention, when the first hydrogenation reaction process R10 is a coal hydrogenation direct liquefaction reaction process, the flushing oil WS can be solid-free distillate oil from the outside of the coal hydrogenation direct liquefaction device, and is used for the initial start-up process and the shutdown process of the coal hydrogenation direct liquefaction device, and the intermediate operation process and the emergency interlocking cutting-off process of the coal hydrogenation direct liquefaction device.
According to the invention, when the first hydrogenation reaction process R10 is a direct coal hydrogenation liquefaction reaction process, flushing oil WS is used in a pressure reduction system DP of the hot high-oil separation HTPS-L to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and the soft lower limit basic flow R1 of the pressure reduction system DP of the hot high-oil separation is established.
In the invention, when the first hydrogenation reaction process R10 is a coal hydrogenation direct liquefaction reaction process, the flushing oil WS can be solid-free distillate oil obtained by fractionating hot high-molecular oil and is used for an intermediate operation process, an emergency interlocking cutting process and a shutdown process of a coal hydrogenation direct liquefaction device.
According to the invention, the hydrocarbon feedstock R10F may be selected from one or more of the following materials:
firstly, low-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the low-temperature coal tar or the distillate oil thereof, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a hydrogenation process;
secondly, the medium-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the medium-temperature coal tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
thirdly, high-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the high-temperature coal tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
fourthly, coal liquefaction oil obtained in the coal liquefaction process or distillate oil thereof or oil obtained in the thermal processing process of the coal liquefaction oil, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process; the coal liquefaction process is a coal hydrogenation direct liquefaction oil preparation process or an oil-coal co-refining process or a coal hydro-thermal solution process by using hydrogen supply solvent oil;
shale oil or distillate oil thereof or oil products obtained in the thermal processing process of the shale oil or the distillate oil thereof, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
sixthly, ethylene cracking tar or an oil product obtained in the thermal processing process of the ethylene cracking tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
seventhly, thermally cracking tar oil of the petroleum-based wax oil;
eighthly, the petroleum sand base oil or the distillate oil thereof or the oil product obtained in the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
ninthly, petroleum-based heavy oil or an oil product obtained in the thermal processing process of the petroleum-based heavy oil, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
hydrocarbon oil containing aromatic hydrocarbon in the amount over 40 wt% and organic nitrogen in the amount over 0.10 wt%.
According to the invention, the first hydrogenation reaction process R10 can be selected from one or more of the following hydrogenation reaction processes:
the coal hydrogenation direct liquefaction oil preparation process adopts a coal hydrogenation direct liquefaction oil preparation process or an oil-coal co-refining process or a coal hydro-thermal solution process by using hydrogen supply solvent oil;
a hydrogenation process of the medium-low temperature coal tar or distillate oil thereof or oil products obtained in the thermal processing process of the medium-low temperature coal tar by using an up-flow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
thirdly, a hydrogenation process of the high-temperature coal tar or distillate oil thereof or oil products obtained in the thermal processing process of the high-temperature coal tar by using an up-flow 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;
the hydrogenation process of the shale oil or the distillate oil thereof or the oil product obtained in the thermal processing process of the shale oil or the distillate oil thereof by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
fifthly, the hydrogenation process of the ethylene cracking tar by using an upflow expansion bed;
sixthly, a hydrogenation process of an oil product obtained in the thermal processing process of the petroleum base heavy oil by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
seventhly, performing hydrogenation on the oil product obtained by the thermal processing process of the petroleum sand based on the heavy oil by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
the hydrogenation process of hydrocarbon oil with arene content over 40 wt% and organic nitrogen content over 0.10 wt% in upflow expanded bed.
In the present invention, the operating conditions are generally:
(1) in the 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 the first hydrogenation reaction effluent R10P accounts for 5-40% of the weight of solids plus the weight of conventional liquid hydrocarbons;
(3) the operating pressure PB of the outlet of the pressure reducer DPV used in the hot high-oil separation pressure reduction system DP is usually less than 2-70% of the operating pressure PA in the hot high-pressure separation process, generally 5-60% of the operating pressure PA in the hot high-pressure separation process, and preferably 10-25% of the operating pressure PA in the hot high-pressure separation process.
In the invention, the basic flow R1 is usually 5-20% of the flow of the thermal high-oil separation HTPS-L.
Drawings
Fig. 1 is a schematic diagram of a principle flow of a soft start-stop method of a hot high-pressure oil separation depressurization system containing a solid hydrogenation product according to the present invention, including a hot high-pressure separator THPSE containing a coal hydrogenation direct liquefaction reaction product R10P, a hot high-pressure oil separation emergency cut self-protection valve FSV, a hot high-pressure separator liquid level regulating valve CV, a hot low-pressure separation part TLPS, and a hot low-pressure oil separation part FRAC 1.
As shown in FIG. 1, the direct coal hydrogenation 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 a pipeline 153 and hot high-pressure oil THPS-L conveyed along a pipeline 155; flushing oil WS is conveyed through a pipeline 190, is mixed with hot high-pressure oil separation THPS-L to form a feed FSV-F of a hot high-pressure oil separation emergency cut-off valve FSV conveyed along a pipeline 156, flows through the emergency cut-off valve FSV and then is conveyed along a pipeline 157, flows through a hot high-pressure separator liquid level regulating valve CV and then is conveyed along a pipeline 158 to serve as a low-pressure separator TLPS feed TLPS-F, enters a hot low-pressure separation part TLPSE through a pipeline 158 and is separated into hot low-pressure gas separation TLPS-V conveyed along a pipeline 163 and hot low-pressure oil separation TLPS-L conveyed along a pipeline 165; the hot low-fraction oil TLPS-L enters a hot low-fraction oil fractionation part FRAC1 through a pipeline 165 to be separated or fractionated to obtain narrow distillate oil, and fig. 1 shows the narrow distillate oil XP01 (such as the distillate oil with the conventional boiling point lower than 200 ℃) conveyed along a pipeline 171, the narrow distillate oil XP02 (such as the distillate oil with the conventional boiling point between 200 and 330 ℃) conveyed along a pipeline 172, the narrow distillate oil XP03 (such as the distillate oil with the conventional boiling point between 330 and 530 ℃) conveyed along a pipeline 173, the narrow distillate oil XP04 (such as the residue with the conventional boiling point higher than 530 ℃) conveyed along a pipeline 174 and the like.
As shown in fig. 1, the source of the flushing oil WS is at least:
firstly, the solid-free distillate oil which is conveyed along a pipeline 180 from the outside of the direct coal hydrogenation liquefaction device can be used for the initial start-up process and the shutdown process of the direct coal hydrogenation liquefaction device; the method can be used for the intermediate operation process and the emergency interlocking cutting-off process of the direct coal hydrogenation liquefaction device;
and the solid-free distillate oil obtained by fractionating the hot high-temperature separation oil can be used in the middle operation process, the emergency interlocking cutting-off process and the shutdown process of the coal hydrogenation direct liquefaction device and is conveyed along the pipeline 212, the pipeline 202 and the pipeline 190.
Detailed Description
The pressure in the present invention refers to absolute pressure.
The conventional boiling point of the invention refers to the vapor-liquid equilibrium temperature of a substance at one atmospheric pressure.
The conventional boiling range as referred to herein refers to the conventional boiling range of the distillate fraction.
The specific gravity of the present invention refers to the ratio of the density of a liquid at ordinary pressure and 15.6 ℃ to the density of a liquid at ordinary pressure and 15.6 ℃ unless otherwise specified.
The conventional gaseous hydrocarbon refers to hydrocarbon which is gaseous under conventional conditions, and comprises methane, ethane, propane and butane.
The conventional liquid hydrocarbon refers to hydrocarbon which is liquid under conventional conditions, and includes pentane and hydrocarbon with higher boiling point.
The impurity elements in the invention refer to non-hydrogen, non-carbon and non-metal components in the raw oil, such as oxygen, sulfur, nitrogen, chlorine and the like.
The impurity component in the invention refers to the hydrogenation conversion product of non-hydrocarbon component in the raw oil, such as water, ammonia, hydrogen sulfide, hydrogen chloride and the like.
The middle distillate according to the present invention, which refers to a hydrocarbon fraction suitable for use as diesel and/or naphtha, may be naphtha and/or diesel.
The middle distillate oil component of the present invention refers to a hydrocarbon component suitable for use as diesel and/or naphtha.
The naphtha component of the present invention refers to conventional liquid hydrocarbon components having a conventional boiling point typically below 220 c, typically below 190 c, and especially 165 c.
The diesel component of the present invention refers to conventional liquid hydrocarbons having a conventional boiling point generally between 165-380 deg.C, generally between 190-350 deg.C, and particularly between 220-330 deg.C.
The heavy oil component of the present invention refers to conventional liquid hydrocarbons having a conventional boiling point typically above 300 deg.C, typically above 330 deg.C, and particularly above 370 deg.C. The heavy oil of the present invention may contain a portion of middle distillate.
The pressure reducing valve is installed in any appropriate mode, the speed reducing phase separating bag of the pressure reducer is generally installed in a vertical mode, the lower space of the speed reducing phase separating bag is a liquid phase area, and the upper space of the speed reducing phase separating bag is a gas phase area; at least most of liquid of the phase separation and deceleration is discharged through a liquid flow discharge port, at least most of gas of the phase separation and deceleration is discharged through a gas discharge port pipeline, jet flow discharged by a pressure reducing valve is sprayed to a liquid phase gathering area from the upper part of a liquid phase space, most of liquid and solid in the jet flow are sprayed into the liquid phase to form liquid phase waves, high-speed jet flow forms low-speed dispersion flow after kinetic energy is absorbed by the liquid, the liquid at the front end of an axis in the jet flow impact direction is reflected by a wall surface to form an area with zero flow velocity, the static pressure of the area is high, a static pressure field with rapid rise of static pressure is formed in the liquid deceleration process, resistance is provided, most of jet flow reduces the impact velocity, and meanwhile, the liquid is pushed to move around, so.
The characteristic parts of the present invention are described below.
The invention discloses a soft start-stop method of a hot high-oil-separation depressurization system containing a solid hydrogenation product, which is characterized by comprising the following steps of:
(1) in a first hydrogenation process R10, a hydrocarbon feedstock R10F is subjected to a first hydrogenation reaction R10R in the presence of hydrogen and a first hydrogenation catalyst R10C, if present, to obtain a first hydrogenation reaction effluent R10P comprising hydrogen, low boiling hydrocarbons, high boiling hydrocarbons and solids;
the first hydrogenation reaction process R10 has the function of hydrogenation and/or hydrocracking at least a part of the hydrocarbon raw material R10F;
a first hydrogenation catalyst R10C, which may be present, overall having the function of hydrogenation and/or hydrocracking;
the first hydrogenation reaction R10R comprises at least a portion of a hydrofinishing reaction and/or at least a portion of a hydrothermally cracking reaction;
(2) in the HTPS process, the first hydrogenation reaction effluent R10P is subjected to gas-liquid separation to obtain solid-containing hot high-molecular oil HTPS-L and hot high-molecular gas HTPS-V; a hot high pressure separation process HTPS, possibly using gaseous hydrogen HTPS-HG to contact the liquid feed from the first hydrogenation effluent R10P to remove at least a portion of the low boiling components in the liquid phase;
at least one part of the hot high-oil separation HTPS-L or medium-pressure deaerated oil is used as an erosion material entering a hot high-oil separation depressurization system DP;
(3) in a hot high-oil separation depressurization system DP, a self-protection valve KV with an emergency cut-off function is used, a flow controller CV for regulating the liquid level of a hot high-pressure separator THPSE is used, and a soft start-stop system is arranged;
in a depressurization system DP of the hot high-oil separation HTPS-L, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and establishing a soft lower limit basic flow R1 of the hot high-oil separation depressurization system DP;
the basic flow R1 is smaller than the flow of the thermal high-oil separation HTPS-L;
when the liquid level of the hot high-pressure separator THPSE is too low and the self-protection valve KV of hot high-pressure oil separation is required to be turned off emergently, the turn-off position of the self-protection valve KV is not a zero-flow full-closed valve position, but is not zero and is smaller than a small opening degree corresponding to a flow value of R1, at the moment, the solid-free flushing oil WS is divided into two paths, one path of the solid-free flushing oil WS reversely flows and pushes the hot high-pressure oil separation to return to the hot high-pressure separator THPSE, the other path of the solid-free flushing oil WS flows in the forward direction to flush solids at the positions of a valve seat and a valve core sealing surface of the self-protection valve KV, and after the flushing.
The working mode of the invention is generally as follows:
(3) a soft opening and closing system is arranged in a hot high oil separation depressurization system DP;
in a depressurization system DP of the hot high-oil separation HTPS-L, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and establishing a soft lower limit basic flow R1 of the hot high-oil separation depressurization system DP;
before the first hydrogenation reaction effluent R10P contains solids, firstly, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV to establish a soft lower limit basic flow R1 of a hot high-oil-separation depressurization system DP;
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 an emergency cut-off self-protection valve KV and is kept injected to be in a normal state;
when the first hydrogenation reaction effluent R10P is reduced until the first hydrogenation reaction process R10 is shut down, the solid-free flushing oil WS continuously enters a feeding system of an emergency cut-off self-protection valve KV and is kept injected to be normal;
when the first hydrogenation reaction effluent R10P is reduced until the first hydrogenation reaction process R10 flushing process without solids is carried out, the solid-free flushing oil WS continuously enters a feeding system of an emergency cut-off self-protection valve KV and is kept injected to be in a normal state;
when the liquid level of the high-pressure hot separator THPSE is too low and the requirement for emergency shutdown of the high-pressure hot separator THPSE is met, the shutdown position of the self-protection valve KV is not a zero-flow full-closed valve position, but is not zero and smaller than a small opening corresponding to a flow value R1, at the moment, the solid-free flushing oil WS is divided into two paths, one path of the solid-free flushing oil WS reversely flows and pushes the high-pressure hot separator THPSE to return to the high-pressure hot separator THPSE, the other path of the solid-free flushing oil WS forwardly flows to flush solids at the positions of a valve seat and a valve core sealing surface of the self-protection valve KV, and after the flushing process lasts for a period of time, the self-protection valve KV and the liquid level control valve CV of the.
In the present invention, the flushing oil WS is generally hydrocarbon oil discharged from a reciprocating pump.
In the invention, when the first hydrogenation reaction process R10 is a coal hydrogenation direct liquefaction reaction process, the flushing oil WS can be solid-free distillate oil from the outside of the coal hydrogenation direct liquefaction device, and is used for the initial start-up process and the shutdown process of the coal hydrogenation direct liquefaction device, and the intermediate operation process and the emergency interlocking cutting-off process of the coal hydrogenation direct liquefaction device.
According to the invention, when the first hydrogenation reaction process R10 is a direct coal hydrogenation liquefaction reaction process, flushing oil WS is used in a pressure reduction system DP of the hot high-oil separation HTPS-L to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and the soft lower limit basic flow R1 of the pressure reduction system DP of the hot high-oil separation is established.
In the invention, when the first hydrogenation reaction process R10 is a coal hydrogenation direct liquefaction reaction process, the flushing oil WS can be solid-free distillate oil obtained by fractionating hot high-molecular oil and is used for an intermediate operation process, an emergency interlocking cutting process and a shutdown process of a coal hydrogenation direct liquefaction device.
According to the invention, the hydrocarbon feedstock R10F may be selected from one or more of the following materials:
firstly, low-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the low-temperature coal tar or the distillate oil thereof, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a hydrogenation process;
secondly, the medium-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the medium-temperature coal tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
thirdly, high-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the high-temperature coal tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
fourthly, coal liquefaction oil obtained in the coal liquefaction process or distillate oil thereof or oil obtained in the thermal processing process of the coal liquefaction oil, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process; the coal liquefaction process is a coal hydrogenation direct liquefaction oil preparation process or an oil-coal co-refining process or a coal hydro-thermal solution process by using hydrogen supply solvent oil;
shale oil or distillate oil thereof or oil products obtained in the thermal processing process of the shale oil or the distillate oil thereof, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
sixthly, ethylene cracking tar or an oil product obtained in the thermal processing process of the ethylene cracking tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
seventhly, thermally cracking tar oil of the petroleum-based wax oil;
eighthly, the petroleum sand base oil or the distillate oil thereof or the oil product obtained in the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
ninthly, petroleum-based heavy oil or an oil product obtained in the thermal processing process of the petroleum-based heavy oil, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
hydrocarbon oil containing aromatic hydrocarbon in the amount over 40 wt% and organic nitrogen in the amount over 0.10 wt%.
According to the invention, the first hydrogenation reaction process R10 can be selected from one or more of the following hydrogenation reaction processes:
the coal hydrogenation direct liquefaction oil preparation process adopts a coal hydrogenation direct liquefaction oil preparation process or an oil-coal co-refining process or a coal hydro-thermal solution process by using hydrogen supply solvent oil;
a hydrogenation process of the medium-low temperature coal tar or distillate oil thereof or oil products obtained in the thermal processing process of the medium-low temperature coal tar by using an up-flow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
thirdly, a hydrogenation process of the high-temperature coal tar or distillate oil thereof or oil products obtained in the thermal processing process of the high-temperature coal tar by using an up-flow 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;
the hydrogenation process of the shale oil or the distillate oil thereof or the oil product obtained in the thermal processing process of the shale oil or the distillate oil thereof by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
fifthly, the hydrogenation process of the ethylene cracking tar by using an upflow expansion bed;
sixthly, a hydrogenation process of an oil product obtained in the thermal processing process of the petroleum base heavy oil by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
seventhly, performing hydrogenation on the oil product obtained by the thermal processing process of the petroleum sand based on the heavy oil by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
the hydrogenation process of hydrocarbon oil with arene content over 40 wt% and organic nitrogen content over 0.10 wt% in upflow expanded bed.
In the present invention, the operating conditions are generally:
(1) in the 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 the first hydrogenation reaction effluent R10P accounts for 5-40% of the weight of solids plus the weight of conventional liquid hydrocarbons;
(3) the operating pressure PB of the outlet of the pressure reducer DPV used in the hot high-oil separation pressure reduction system DP is usually less than 2-70% of the operating pressure PA in the hot high-pressure separation process, generally 5-60% of the operating pressure PA in the hot high-pressure separation process, and preferably 10-25% of the operating pressure PA in the hot high-pressure separation process.
In the invention, the basic flow R1 is usually 5-20% of the flow of the thermal high-oil separation HTPS-L.
Claims (14)
1. The soft start-stop method of the hot high-oil-separation depressurization system containing the solid hydrogenation product is characterized by comprising the following steps of:
(1) in a first hydrogenation process R10, a hydrocarbon feedstock R10F is subjected to a first hydrogenation reaction R10R in the presence of hydrogen and a first hydrogenation catalyst R10C, if present, to obtain a first hydrogenation reaction effluent R10P comprising hydrogen, low boiling hydrocarbons, high boiling hydrocarbons and solids;
the first hydrogenation reaction process R10 has the function of hydrogenation and/or hydrocracking at least a part of the hydrocarbon raw material R10F;
a first hydrogenation catalyst R10C, which may be present, overall having the function of hydrogenation and/or hydrocracking;
the first hydrogenation reaction R10R comprises at least a portion of a hydrofinishing reaction and/or at least a portion of a hydrothermally cracking reaction;
(2) in the HTPS process, the first hydrogenation reaction effluent R10P is subjected to gas-liquid separation to obtain solid-containing hot high-molecular oil HTPS-L and hot high-molecular gas HTPS-V; a hot high pressure separation process HTPS, possibly using gaseous hydrogen HTPS-HG to contact the liquid feed from the first hydrogenation effluent R10P to remove at least a portion of the low boiling components in the liquid phase;
at least one part of the hot high-oil separation HTPS-L or medium-pressure deaerated oil is used as an erosion material entering a hot high-oil separation depressurization system DP;
(3) in a hot high-oil separation depressurization system DP, a self-protection valve KV with an emergency cut-off function is used, a flow controller CV for regulating the liquid level of a hot high-pressure separator THPSE is used, and a soft start-stop system is arranged;
in a depressurization system DP of the hot high-oil separation HTPS-L, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and establishing a soft lower limit basic flow R1 of the hot high-oil separation depressurization system DP;
the basic flow R1 is smaller than the flow of the thermal high-oil separation HTPS-L;
when the liquid level of the hot high-pressure separator THPSE is too low and the self-protection valve KV of hot high-pressure oil separation is required to be turned off emergently, the turn-off position of the self-protection valve KV is not a zero-flow full-closed valve position, but is not zero and is smaller than a small opening degree corresponding to a flow value of R1, at the moment, the solid-free flushing oil WS is divided into two paths, one path of the solid-free flushing oil WS reversely flows and pushes the hot high-pressure oil separation to return to the hot high-pressure separator THPSE, the other path of the solid-free flushing oil WS flows in the forward direction to flush solids at the positions of a valve seat and a valve core sealing surface of the self-protection valve KV, and after the flushing.
2. The method of claim 1, further comprising:
(3) a soft opening and closing system is arranged in a hot high oil separation depressurization system DP;
in a depressurization system DP of the hot high-oil separation HTPS-L, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and establishing a soft lower limit basic flow R1 of the hot high-oil separation depressurization system DP;
before the first hydrogenation reaction effluent R10P contains solids, firstly, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV to establish a soft lower limit basic flow R1 of a hot high-oil-separation depressurization system DP;
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 an emergency cut-off self-protection valve KV and is kept injected to be in a normal state;
when the first hydrogenation reaction effluent R10P is reduced until the first hydrogenation reaction process R10 is shut down, the solid-free flushing oil WS continuously enters a feeding system of an emergency cut-off self-protection valve KV and is kept injected to be normal;
when the first hydrogenation reaction effluent R10P is reduced until the first hydrogenation reaction process R10 flushing process without solids is carried out, the solid-free flushing oil WS continuously enters a feeding system of an emergency cut-off self-protection valve KV and is kept injected to be in a normal state;
when the liquid level of the high-pressure hot separator THPSE is too low and the requirement for emergency shutdown of the high-pressure hot separator THPSE is met, the shutdown position of the self-protection valve KV is not a zero-flow full-closed valve position, but is not zero and smaller than a small opening corresponding to a flow value R1, at the moment, the solid-free flushing oil WS is divided into two paths, one path of the solid-free flushing oil WS reversely flows and pushes the high-pressure hot separator THPSE to return to the high-pressure hot separator THPSE, the other path of the solid-free flushing oil WS forwardly flows to flush solids at the positions of a valve seat and a valve core sealing surface of the self-protection valve KV, and after the flushing process lasts for a period of time, the self-protection valve KV and the liquid level control valve CV of the.
3. The method of claim 1, further comprising:
the flushing oil WS is hydrocarbon oil discharged from a reciprocating pump.
4. The method of claim 1, further comprising:
a first hydrogenation reaction process R10, which is a coal hydrogenation direct liquefaction reaction process;
the flushing oil WS is solid-free distillate oil from the outside of the coal hydrogenation direct liquefaction device, is used for the initial start-up process and the shutdown process of the coal hydrogenation direct liquefaction device, and is used for the intermediate operation process and the emergency interlocking cutting-off process of the coal hydrogenation direct liquefaction device.
5. The method of claim 1, further comprising:
a first hydrogenation reaction process R10, which is a coal hydrogenation direct liquefaction reaction process;
in a depressurization system DP of the hot high-oil separation HTPS-L, flushing oil WS is used to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and a soft lower limit basic flow R1 of the depressurization system DP of the hot high-oil separation is established.
6. The method of claim 1, further comprising:
a first hydrogenation reaction process R10, which is a coal hydrogenation direct liquefaction reaction process;
the flushing oil WS is solid-free distillate oil obtained by fractionating hot high-molecular oil and is used for the intermediate operation process, the emergency interlocking cutting-off process and the shutdown process of the coal hydrogenation direct liquefaction device.
7. The method of claim 1, further comprising:
the hydrocarbon raw material R10F is selected from one or more of the following materials:
firstly, low-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the low-temperature coal tar or the distillate oil thereof, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a hydrogenation process;
secondly, the medium-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the medium-temperature coal tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
thirdly, high-temperature coal tar or distillate oil thereof or oil obtained in the thermal processing process of the high-temperature coal tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
fourthly, coal liquefaction oil obtained in the coal liquefaction process or distillate oil thereof or oil obtained in the thermal processing process of the coal liquefaction oil, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process; the coal liquefaction process is selected from the oil-coal co-refining process and the coal hydro-thermal solution process;
shale oil or distillate oil thereof or oil products obtained in the thermal processing process of the shale oil or the distillate oil thereof, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
sixthly, ethylene cracking tar or an oil product obtained in the thermal processing process of the ethylene cracking tar, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
seventhly, thermally cracking tar oil of the petroleum-based wax oil;
eighthly, the petroleum sand base oil or the distillate oil thereof or the oil product obtained in the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
ninthly, petroleum-based heavy oil or an oil product obtained in the thermal processing process of the petroleum-based heavy oil, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
hydrocarbon oil containing aromatic hydrocarbon in the amount over 40 wt% and organic nitrogen in the amount over 0.10 wt%.
8. The method of claim 1, further comprising:
the first hydrogenation reaction process R10 is selected from one or more of the following hydrogenation reaction processes:
the process of directly liquefying coal to prepare oil by coal hydrogenation comprises an oil-coal co-refining process and a coal hydro-thermal solution process;
a hydrogenation process of the medium-low temperature coal tar or distillate oil thereof or oil products obtained in the thermal processing process of the medium-low temperature coal tar by using an up-flow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
thirdly, a hydrogenation process of the high-temperature coal tar or distillate oil thereof or oil products obtained in the thermal processing process of the high-temperature coal tar by using an up-flow 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;
the hydrogenation process of the shale oil or the distillate oil thereof or the oil product obtained in the thermal processing process of the shale oil or the distillate oil thereof by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
fifthly, the hydrogenation process of the ethylene cracking tar by using an upflow expansion bed;
sixthly, a hydrogenation process of an oil product obtained in the thermal processing process of the petroleum base heavy oil by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
seventhly, performing hydrogenation on the oil product obtained by the thermal processing process of the petroleum sand based on the heavy oil by using an upflow expansion bed, wherein the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process;
the hydrogenation process of hydrocarbon oil with arene content over 40 wt% and organic nitrogen content over 0.10 wt% in upflow expanded bed.
9. The method of claim 1, further comprising:
(1) in the 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 the first hydrogenation reaction effluent R10P accounts for 5-40% of the weight of solids plus the weight of conventional liquid hydrocarbons;
(3) the operating pressure PB of the outlet of the pressure reducer DPV used in the hot high-oil separation pressure reduction system DP is less than 2-70% of the operating pressure PA in the hot high-pressure separation process.
10. The method of claim 9, further comprising:
(3) the operating pressure PB of the outlet of the pressure reducer DPV used in the hot high-oil separation pressure reduction system DP is 5-60% of the operating pressure PA in the hot high-pressure separation process.
11. The method of claim 9, further comprising:
(3) the operating pressure PB of the outlet of the pressure reducer DPV used in the hot high-oil separation pressure reduction system DP is 10-25% of the operating pressure PA in the hot high-pressure separation process.
12. The method of claim 1, further comprising:
(3) a soft opening and closing system is arranged in a hot high oil separation depressurization system DP;
in a depressurization system DP of the hot high-oil separation HTPS-L, using solid-free flushing oil WS to enter a feeding system of an emergency cut-off self-protection valve KV of the hot high-oil separation HTPS-L, and establishing a soft lower limit basic flow R1 of the hot high-oil separation depressurization system DP;
the basic flow R1 is 5-20% of the flow of the thermal high-oil separation HTPS-L.
13. The method of claim 1, further comprising:
the hydrocarbon raw material R10F is coal liquefied oil obtained in the process of directly liquefying coal to prepare oil by hydrogenation of hydrogen-donating solvent oil or distillate oil thereof or oil obtained in the process of thermal processing thereof, and the thermal processing process is a heavy oil coking process, a heavy oil catalytic cracking process or a heavy oil hydrogenation process.
14. The method of claim 1, further comprising:
the first hydrogenation reaction process R10 is a coal hydrogenation direct liquefaction oil making process using hydrogen supply solvent oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710149329.8A CN108504379B (en) | 2017-02-28 | 2017-02-28 | Soft start-stop method of hot high-oil-separation depressurization system containing solid hydrogenation products |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710149329.8A CN108504379B (en) | 2017-02-28 | 2017-02-28 | Soft start-stop method of hot high-oil-separation depressurization system containing solid hydrogenation products |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108504379A CN108504379A (en) | 2018-09-07 |
| CN108504379B true CN108504379B (en) | 2020-12-01 |
Family
ID=63373447
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710149329.8A Active CN108504379B (en) | 2017-02-28 | 2017-02-28 | Soft start-stop method of hot high-oil-separation depressurization system containing solid hydrogenation products |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108504379B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110846073B (en) * | 2018-08-20 | 2023-05-02 | 何巨堂 | Flushing method of main hot high-pressure oil separator containing solid product in hydrocarbon material hydrogenation process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5964985A (en) * | 1994-02-02 | 1999-10-12 | Wootten; William A. | Method and apparatus for converting coal to liquid hydrocarbons |
| JP2006225425A (en) * | 2005-02-15 | 2006-08-31 | Hitachi Ltd | Heavy oil reforming apparatus |
| CN104633134A (en) * | 2015-02-10 | 2015-05-20 | 无锡智能自控工程股份有限公司 | Hydrocracking heat highly-distributing high-pressure regulating angle valve |
| CN105623703A (en) * | 2016-01-19 | 2016-06-01 | 何巨堂 | Thermal high-pressure dissociating gas dust removal method for three-phase product of hydrocarbon material hydrogenation reaction |
| CN105647576A (en) * | 2015-12-30 | 2016-06-08 | 何巨堂 | Method for performing combined hydro-upgrading on high aromatic hydrocarbon after high-pressure gas stripping separation |
-
2017
- 2017-02-28 CN CN201710149329.8A patent/CN108504379B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5964985A (en) * | 1994-02-02 | 1999-10-12 | Wootten; William A. | Method and apparatus for converting coal to liquid hydrocarbons |
| JP2006225425A (en) * | 2005-02-15 | 2006-08-31 | Hitachi Ltd | Heavy oil reforming apparatus |
| CN104633134A (en) * | 2015-02-10 | 2015-05-20 | 无锡智能自控工程股份有限公司 | Hydrocracking heat highly-distributing high-pressure regulating angle valve |
| CN105647576A (en) * | 2015-12-30 | 2016-06-08 | 何巨堂 | Method for performing combined hydro-upgrading on high aromatic hydrocarbon after high-pressure gas stripping separation |
| CN105623703A (en) * | 2016-01-19 | 2016-06-01 | 何巨堂 | Thermal high-pressure dissociating gas dust removal method for three-phase product of hydrocarbon material hydrogenation reaction |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108504379A (en) | 2018-09-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP3374470B1 (en) | Method to remove metals from petroleum | |
| US9771530B2 (en) | Integrated slurry hydroprocessing and steam pyrolysis of crude oil to produce petrochemicals | |
| US20080307827A1 (en) | Method of refining natural gas and natural gas refining system | |
| US20140001097A1 (en) | Process for the recovery of crude | |
| CN108504379B (en) | Soft start-stop method of hot high-oil-separation depressurization system containing solid hydrogenation products | |
| US20230202841A1 (en) | Integrated hydrogen production and bio-renewable conversion process | |
| CN116261586A (en) | Integrated continuous conversion and separation process for upgrading mixed plastic waste to clean gasoline and diesel fuel and other products | |
| CN105273751B (en) | The separator combined system and its design method and purposes of a kind of Multiple Optimization | |
| CN105542852B (en) | A kind of synthetic process of high density hydrocarbon | |
| CN105441128B (en) | The temperature control method and its design method and purposes of a kind of hydrogenation technique | |
| CN110846073B (en) | Flushing method of main hot high-pressure oil separator containing solid product in hydrocarbon material hydrogenation process | |
| CN107163975B (en) | A kind of device and method of lighter hydrocarbons depth recycling | |
| CN108504383A (en) | The deceleration split-phase guidance system that the choke zone gas-liquid injection stream of reducing transformer uses | |
| JP6853417B2 (en) | Cooling method for pyrolysis products | |
| CN108424783B (en) | Method for reducing pressure of absorption liquid material used for pressure material containing erosion easy-vaporization component | |
| CN113122314A (en) | Gas-liquid separation process for hydrogenation reaction product | |
| CN112707785B (en) | Pyrolysis gas separation system with cold energy recovery function and separation method | |
| US11162035B2 (en) | Catalytic upgrading of heavy oil with supercritical water | |
| KR102658017B1 (en) | Supercritical water process to produce bottom-free hydrocarbons | |
| CN105542837A (en) | Step-by-step pressure reduction method of three-phase fluid as well as design method and application thereof | |
| CN106187665B (en) | The method of absorption and separation isobutene device lighter hydrocarbons | |
| CN114478160A (en) | Method and system for preparing low-carbon olefin from crude oil | |
| CN105694968A (en) | Reverse feed high-aromatic-hydrocarbon hydro-upgrading method | |
| CN116135951A (en) | Control method of communicating vessel for hydrocarbon material up-flow expanded bed grading serial hydrogenation reaction process | |
| CN114478159A (en) | Method and system for preparing low-carbon olefin |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20190411 Address after: 471003 Ruize Building 2107, 215 Heluo Road, Luoyang High-tech Development Zone, Luoyang China (Henan) Free Trade Experimental Zone, Henan Province Applicant after: Luoyang Rui Hua new energy technology development Co., Ltd. Address before: 471003 room 1503, Shen Tai Building, south section of Nanchang Road, Jianxi District, Luoyang, Henan Applicant before: He Jutang Applicant before: Guo Kai Applicant before: Li Bo |
|
| TA01 | Transfer of patent application right | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |