CN114456828B - Thick oil flow cavitation viscosity reduction system and process method - Google Patents
Thick oil flow cavitation viscosity reduction system and process method Download PDFInfo
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- CN114456828B CN114456828B CN202111570236.5A CN202111570236A CN114456828B CN 114456828 B CN114456828 B CN 114456828B CN 202111570236 A CN202111570236 A CN 202111570236A CN 114456828 B CN114456828 B CN 114456828B
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- 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
- C10G15/00—Cracking of hydrocarbon oils by electric means, electromagnetic or mechanical vibrations, by particle radiation or with gases superheated in electric arcs
- C10G15/08—Cracking of hydrocarbon oils by electric means, electromagnetic or mechanical vibrations, by particle radiation or with gases superheated in electric arcs by electric means or by electromagnetic or mechanical vibrations
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- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/302—Viscosity
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Abstract
The invention relates to a thick oil liquid flow cavitation viscosity reduction system and a process method, and the technical scheme is as follows: when a thick oil storage tank is adopted to supply thick oil, a hydrogen supply agent storage tank can be communicated with the thick oil storage tank, the hydrogen supply agent and the thick oil are mixed and then are conveyed to a high-pressure plunger device through a low-pressure supply pump, the mixed liquid is pressurized and then is injected into a cavitation treatment device, the viscosity of the thick oil is reduced by utilizing the liquid flow cavitation effect, then the thick oil after viscosity reduction is injected into the storage tank for storage and standby, and the treated thick oil can also be gathered into a gathering and conveying pipeline for conveying. The beneficial effects are that: the viscosity reduction treatment method disclosed by the invention is used for performing viscosity reduction treatment on the thick oil by utilizing the microscopic-scale extreme environments such as high temperature, high pressure and the like generated by cavitation effect, the reaction condition is mild, meanwhile, the cavitation effect can be used for performing viscosity reduction in a pure physical mode, the viscosity reduction treatment method can be integrated with the methods such as heating viscosity reduction, thin oil mixing viscosity reduction, chemical agent adding viscosity reduction and the like for use, the viscosity of the treated thick oil is basically not recovered, and the method is particularly suitable for industrial application.
Description
Technical Field
The invention relates to the field of thickened oil modification and gathering and transportation, in particular to a thickened oil liquid flow cavitation viscosity reduction system and a process method.
Background
The proportion of the thickened oil in the petroleum resources in China is more than 20 percent, and the ratio of the thickened oil to the petroleum resources in China is 79.5 multiplied by 10 8 The development and utilization of the heavy oil have great potential, and the heavy oil has great significance for meeting the energy demand of the long-term development of China, but the heavy oil is a complex and multi-component mixture and contains a large amount of colloid and asphaltene, and because the colloid and the asphaltene have high carbon content, large average molecular weight and long carbon chain length, the interaction force among the molecules of the colloid and the asphaltene is increased, and the colloid and the asphaltene are also the main reason of the high viscosity of the heavy oil; the development and the gathering and transportation of the thick oil are difficult due to the high viscosity and the low fluidity of the thick oil, so that the key point of the high-efficiency development and utilization of the thick oil is the viscosity reduction treatment of the thick oil.
In the current industrial system of China, the main ways of reducing the viscosity of the thick oil are as follows:
(1) Blending thin oil for viscosity reduction: the method is always the main method for reducing viscosity, reducing drag and conveying the thick oil, and has the advantages of simplicity and effectiveness, but the method needs to ensure enough thin oil sources and has higher cost.
(2) Heating and viscosity reduction: the viscosity of the thickened oil is very sensitive relative to the temperature, and within a certain temperature range, the viscosity of the thickened oil is obviously reduced when the temperature is increased, and the viscosity of the thickened oil is reduced by about half when the temperature is increased by 10 ℃; when the long chain structure in the thick oil is completely destroyed, the viscosity of the thick oil is reduced very little along with the rise of the temperature, namely, the temperature is continuously raised and the viscosity of the thick oil is reduced very little when exceeding a certain temperature range, and meanwhile, the method has larger energy consumption.
(3) Ultrasonic viscosity reduction: the cavitation effect, the mechanical effect and the thermal effect generated under the ultrasonic excitation are utilized to break the long chain in the thickened oil, and the thickened oil is promoted to generate corresponding physical and chemical changes, so that the viscosity of the thickened oil is reduced, and the fluidity of the thickened oil is increased.
(4) Surfactant/oil-soluble treating agent viscosity reduction: the method is similar to a viscosity reduction method by blending thin oil, and simultaneously needs a large amount of surfactant, so that the cost is high.
(5) High-temperature catalytic cracking viscosity reduction: under the condition of high-temperature catalytic cracking reaction, after the thick oil macromolecules undergo catalytic reaction, the viscosity of the thick oil macromolecules can be irreversibly reduced obviously, and the effect is obvious.
(6) Viscosity reduction by microorganisms: the microbes degrade long-chain saturated hydrocarbon into medium-short-chain hydrocarbon, so that the average molecular chain of the saturated hydrocarbon is shortened, and the viscosity of the thickened oil is reduced; the microorganisms act on colloid and asphaltene to generate long-chain molecular fatty acid, carbonyl-containing compounds and other biological surface active substances, reduce the oil-water interfacial tension, emulsify thick oil and reduce the viscosity of the thick oil; the method is generally applied to the field of improving the seepage characteristics of underground thick oil, takes a long time to take effect and is not suitable for ground gathering and transportation of the thick oil.
In summary, the existing viscosity reduction methods for thick oil have advantages and disadvantages, and cannot be replaced by each other, but a special technology needs to be sought for a specific field from the aspects of cost, operability and applicability so as to achieve the best cost performance.
Disclosure of Invention
The invention aims to provide a thick oil flow cavitation viscosity reduction system and a thick oil flow cavitation viscosity reduction process method aiming at the defects in the prior art, wherein the viscosity reduction treatment is carried out on thick oil by utilizing micro-scale high temperature and high pressure generated by cavitation effect; the invention can not only use cavitation effect to carry out viscosity reduction on the thick oil in a pure physical mode, but also can be integrated with methods of viscosity reduction by heating, viscosity reduction by mixing with thin oil, viscosity reduction by adding chemical agents and the like, and is particularly suitable for large-scale industrial application.
The invention provides a thick oil liquid flow cavitation viscosity reduction process method, which adopts the technical scheme that: the device comprises a thickened oil storage tank (L1), a hydrogen supply agent storage tank (L2), a low-pressure feed pump (L3), a high-pressure plunger device (L4), a cavitation treatment device (L5), a thickened oil injection storage tank (L6) and a thickened oil gathering and transportation pipeline (L8), wherein when the thickened oil storage tank (L1) is used for supplying thickened oil, the hydrogen supply agent storage tank (L2) can be communicated with the thickened oil storage tank (L1), the hydrogen supply agent and the thickened oil are mixed and then are conveyed to the high-pressure plunger device (L4) through the low-pressure feed pump (L3), the mixed liquid is pressurized and then injected into the cavitation treatment device (L5), the viscosity of the thickened oil is reduced by using a liquid flow cavitation effect, the thickened oil after viscosity reduction is injected into the storage tank (L6) for storage and standby, and the treated thickened oil is gathered into the gathering and transportation pipeline (L8) for conveying;
when the viscosity reduction system is used as a side branch of a thick oil gathering and transportation pipeline (L8), the gathering and transportation pipeline (L8) directly supplies materials to the high-pressure plunger device (L4), and the viscosity is reduced by the cavitation treatment device (L5) and then stored in the storage tank or directly collected into the gathering and transportation pipeline (L8).
Preferably, the cavitation treatment device (L5) comprises a cavitation nozzle assembly (L5-1) and a target plate assembly (L5-2), wherein the target plate assembly (L5-2) is positioned at one side of the cavitation nozzle assembly (L5-1) and forms a low-speed high-pressure area (Q1), a high-speed low-pressure area (Q2), an expansion area (Q3) and a cavitation collapse area (Q4);
thickened oil flows in from cavitation nozzle subassembly (L5-1) left side, gets into low-speed high-pressure area (Q1), flows out from the right side, gets into high-speed low-pressure area (Q2), because of the aperture narrows, forms the efflux at high-speed low-pressure area (Q2) district right side exit, has two low-pressure areas to form around the efflux formation: one is a tangential region (Q2-1) when the jet is formed, and the other is a vortex region (Q2-2) when the jet enters a relatively static fluid; when the jet flow continues to develop forwards and enters the expansion area (Q3), under certain conditions, the pressure in the expansion area (Q3) is lower than the necessary pressure for the gas nucleus to be stable, namely the saturated vapor pressure of the liquid at the temperature, the gas nucleus in the liquid grows and rapidly forms large cavitation bubbles filled with vapor, and after the cavitation bubbles enter the cavitation bubble collapse area (Q4), the cavitation bubbles collapse and collapse due to the sudden increase of the pressure or the movement of the cavitation bubbles to the vicinity of the target plate, so that the cavitation effect is generated;
the collapse of the cavitation bubble generates a very short strong pressure pulse, a tiny space around the bubble generates an extreme high-temperature and high-pressure microenvironment, the local temperature of the microenvironment can reach 1900-5000K, the pressure of the microenvironment exceeds 5 multiplied by 107Pa, and the local temperature is accompanied by strong shock waves and micro jet flow with the speed per hour as high as 400 m/s. Under the extreme environment, under the physical and chemical actions of mechanical shearing, pyrolysis, radical oxidation and supercritical water oxidation, the colloid structure of the thick oil is damaged, colloid and asphaltene macromolecules in the thick oil can generate reactions such as chain scission, cracking and hydrogenation, the macromolecules are changed into micromolecules, the molecular mass is reduced, and the viscosity is reduced.
The thick oil liquid flow cavitation viscosity reduction system provided by the invention has the technical scheme that: comprises a feeding system (2), a control and power system (3), a cavitation treatment system (4) and a storage system (5),
the feeding system (2) comprises a hydrogen supply agent storage tank (2-2), a hydrogen supply agent feeding pump (2-3), a tail gas absorption tank (2-4), a stirrer (2-5), a storage tank heater (2-6) and a thick oil storage tank (2-7), wherein the hydrogen supply agent feeding pump (2-3) is arranged at the lower end of the hydrogen supply agent storage tank (2-2) and is connected to the thick oil storage tank (2-7) through a pipeline, the stirrer (2-5) is arranged in the thick oil storage tank (2-7), the tail gas absorption tank (2-4) is arranged at the upper part of the thick oil storage tank (2-7), the stirrer (2-5) is connected and controlled with the power system (3) through control, and the output end of the thick oil storage tank (2-7) is connected to the cavitation treatment system (4) through a pipeline;
the cavitation treatment system (4) comprises a variable frequency motor (4-1), a high-pressure plunger pump (4-2) and a cavitation processor (4-7), the input end of the cavitation processor (4-7) is connected with the high-pressure plunger pump (4-2) and the variable frequency motor (4-1), and the output end of the cavitation processor is connected with the storage system (5);
the storage system (5) comprises a first stirrer (5-1), a second stirrer (5-2), a first product tank (5-3) and a second product tank (5-4), thick oil subjected to cavitation treatment is sent to the first product tank (5-3) or the second product tank (5-4), the first stirrer (5-1) is arranged in the first product tank (5-3), and the second stirrer (5-2) is arranged in the second product tank (5-4).
Preferably, the cavitation processor (4-7) comprises a liquid inlet pipe (4-7-1), a front cover plate (4-7-2), a high-temperature oil-resistant seal (4-7-3), a front end cover (4-7-4), a cavitation nozzle (4-7-5), a reactor cavity (4-7-6), a target plate (4-7-7), a driving nut (4-7-8), a spray distance adjusting rod (4-7-9), an adjusting handle (4-7-10), a rear cover plate (4-7-11), a rear end cover (4-7-12), a bearing (4-7-13), a liquid outlet pipe (4-7-14), a high-pressure tee (4-7-15), a sampling port valve (4-7-16), a delivery pipe valve (4-7-17), a delivery pipe (4-7-18), a pull rod (4-7-19) and a fastening nut (4-7-20);
the front end cover (4-7-4) is buckled and pressed in a groove at the right side of the front cover plate (4-7-2) and is arranged at the left side of the reactor cavity (4-7-6) at the same time; the rear end cover (4-7-12) is buckled and pressed in a groove at the left side of the rear cover plate (4-7-11) and is connected with the right side of the reactor cavity (4-7-6) through threads, and the structure is connected into a closed pressure container through a plurality of pull rods (4-7-19) and fastening nuts (4-7-20); the liquid inlet pipe (4-7-1) is fixed on the front end cover (4-7-4), is rotatably connected with the cavitation nozzle (4-7-5) through threads and is placed in a closed pressure vessel; the spray distance adjusting rod (4-7-9) and the driving nut (4-7-8) form a spiral adjusting structure, wherein the left side of the spray distance adjusting rod (4-7-9) is connected with the target plate (4-7-7) in a screwing manner, the driving nut (4-7-8) is supported on the right side of the reactor cavity (4-7-6) through a bearing (4-7-13) to form a revolute pair, and the distance between the target plate (4-7-7) and the outlet end of the cavitation nozzle (4-7-5) is adjusted through rotating the adjusting handle (4-7-10); the left side of the reactor cavity (4-7-6) is provided with a liquid outlet pipe (4-7-14), the treated thickened oil can be conveyed to a conveying pipe valve (4-7-17) through a high-pressure tee joint (4-7-15) and is conveyed out through a conveying pipe (4-7-18), and in addition, thickened oil sampling analysis can be carried out at the position of a sampling port valve (4-7-16).
Preferably, the cavitation nozzle (4-7-5) is formed by sequentially connecting a first-stage cavitation nozzle (4-7-5-1), a first-stage transition joint (4-7-5-2), a second-stage cavitation nozzle (4-7-5-3), a second-stage transition joint (4-7-5-4), a third-stage cavitation nozzle (4-7-5-5) and a tail end nozzle (4-7-5-6), and is respectively provided with a high-temperature oil-resistant seal (4-7-5-7), and the cavitation nozzles at all stages are connected with the transition joints at all stages through screwing.
Preferably, the feeding system (2) further comprises a high-pressure four-way joint (2-1), a pipeline heater (2-12) and a pipeline buffer (2-13), the thick oil is connected with the high-pressure four-way joint (2-1) through the gathering and transportation pipeline (1), one output end of the high-pressure four-way joint (2-1) is connected to the thick oil storage tank (2-7) through a pipeline, the other output end of the high-pressure four-way joint (2-1) is connected to the pipeline heater (2-12) and the pipeline buffer (2-13) through a pipeline, and the output end of the pipeline buffer (2-13) is connected to the cavitation processor (4-7).
Preferably, the primary cavitation nozzle (4-7-5-1), the secondary cavitation nozzle (4-7-5-3) and the tertiary cavitation nozzle (4-7-5-5) have an inlet cone angle α 1= α 2= α 3=13.5 °, and the ratio of the outlet diameters is: d1: d2: d3= 2.
Preferably, the ratio of the outlet diameters of the primary transition joint (4-7-5-2), the secondary transition joint (4-7-5-4) and the end nozzle (4-7-5-6) is: d4: d5: d6= 2; the ratio of the diameter of the outlet of the first-stage cavitation nozzle (4-7-5-1) to the diameter of the inlet of the first-stage transition joint (4-7-5-2) is as follows: d1: d4= 1; the ratio of the diameter of the outlet of the secondary cavitation nozzle (4-7-5-3) to the diameter of the inlet of the secondary transition joint (4-7-5-4) is as follows: d2: d5= 3; the ratio of the outlet diameter of the three-stage cavitation nozzle (4-7-5-5) to the outlet diameter of the tail end nozzle (4-7-5-6) is as follows: d3: d6= 2.
Compared with the prior art, the invention has the following beneficial effects:
(1) The liquid flow cavitation bubble collapse can generate extreme high temperature and high pressure conditions, so the liquid flow cavitation viscous oil viscosity reduction technology can carry out viscosity reduction treatment under mild conditions, has simple equipment requirement and convenient operation, and avoids the harsh conditions of catalytic cracking of the viscous oil;
(2) The technology can be directly applied to a thick oil exploitation well head, carries out primary viscosity reduction treatment on the extracted thick oil, and has higher thick oil treatment efficiency and treatment capacity and low energy consumption;
(3) The viscosity reduction of the liquid flow cavitation thickened oil can be carried out on the basis of no or little addition of a hydrogen donor, so that the pollution to the thickened oil is avoided, the applicability is wide, and the cost is low;
(4) The viscosity of the thickened oil subjected to liquid flow cavitation treatment can not be recovered basically, so that the viscosity of the thickened oil can be reduced permanently, and the condition that the viscosity of the thickened oil is increased in the long-distance conveying process is avoided.
Drawings
FIG. 1 is a schematic flow chart of the present invention;
FIG. 2 is a schematic diagram of the principle of cavitation effect of the present invention;
FIG. 3 is a flowchart illustrating the full domain process of the present invention;
FIG. 4 is a process flow diagram of the feeding system of the present invention;
FIG. 5 is a process flow diagram of the cavitation processing system of the present invention;
FIG. 6 is a schematic view of the cavitation processor in the global domain;
FIG. 7 is a right side view of the cavitation processor of the present invention;
FIG. 8 is a left side view of the cavitation processor of the present invention;
FIG. 9 is a schematic structural view of a cavitation nozzle assembly of the present invention;
FIG. 10 is a process flow diagram of a memory system of the present invention;
in the upper diagram: a thickened oil storage tank L1, a hydrogen supply agent storage tank L2, a low-pressure feed pump L3, a high-pressure plunger device L4, a cavitation treatment device L5, a thickened oil injection storage tank L6, a thickened oil gathering and transportation pipeline L8, a low-speed high-pressure area Q1, a high-speed low-pressure area Q2, an expansion area Q3, a cavitation collapse area Q4, a tangential area Q2-1 and an eddy area Q2-2,
a gathering and transportation pipeline 1, a material supply system 2, a control and power system 3, a cavitation processing system 4 and a storage system 5,
2-1 high-pressure four-way joint, 2-2 hydrogen supply agent storage tank, 2-3 hydrogen supply agent feeding pump, 2-4 tail gas absorption tank, 2-5 stirrer, 2-6 storage tank heater, 2-7 thick oil storage tank, 2-8 slurry feeding pump, 2-9 first standby slurry feeding pump, 2-10 second standby slurry feeding pump, 2-11 flowmeter, 2-12 pipeline heater, 2-13 pipeline buffer, S21 stop valve, S22 stop valve, S23 stop valve, S24 stop valve, S25 stop valve, S26 stop valve, S27 stop valve, S28 stop valve, T21 one-way valve, T22 one-way valve, T23 one-way valve T24,
4-1 of variable frequency motor, 4-2 of high pressure plunger pump, 4-3 of standby variable frequency motor, 4-4 of standby high pressure plunger pump, 4-5 of pressure gauge, 4-6 of standby pressure gauge, 4-7 of cavitation processor, 4-8 of standby cavitation processor, 4-9 of overflow pipeline, 4-10 of standby overflow pipeline, stop valve S41, stop valve S42, stop valve S43, stop valve S44, stop valve S45, stop valve S46, safety overflow valve Y41 and safety overflow valve Y42,
4-7-1 of liquid inlet pipe, 4-7-2 of front cover plate, 4-7-3 of high-temperature oil-resistant seal, 4-7-4 of front end cover, 4-7-5 of cavitation nozzle, 4-7-6 of reactor cavity, 4-7-7 of target plate, 4-7-8 of driving nut, 4-7-9 of spray distance adjusting rod, 4-7-10 of adjusting handle, 4-7-11 of rear cover plate, 4-7-12 of rear end cover, 4-7-13 of bearing, 4-7-14 of liquid outlet pipe, 4-7-15 of high-pressure tee joint, 4-7-16 of sampling port valve, 4-7-17 of delivery pipe valve, 4-7-18 of delivery pipe, 4-7-19 of pull rod and 4-7-20 of fastening nut,
4-7-5-1 of a first-stage cavitation nozzle, 4-7-5-2 of a first-stage transition joint, 4-7-5-3 of a second-stage cavitation nozzle, 4-7-5-4 of a second-stage transition joint, 4-7-5-5 of a third-stage cavitation nozzle, 4-7-5-6 of a tail end nozzle and 4-7-5-7 of a high-temperature oil-resistant seal,
a first stirrer 5-1, a second stirrer 5-2, a first product tank 5-3 and a second product tank 5-4.
Detailed Description
The preferred embodiments of the present invention will be described in conjunction with the accompanying drawings, and it will be understood that they are described herein for the purpose of illustration and explanation and not limitation.
Embodiment 1, the invention provides a thick oil liquid flow cavitation viscosity reduction process method, which has the technical scheme that: the device comprises a thickened oil storage tank L1, a hydrogen supply agent storage tank L2, a low-pressure feed pump L3, a high-pressure plunger device L4, a cavitation treatment device L5, a thickened oil injection storage tank L6 and a thickened oil gathering and transportation pipeline L8, wherein when the thickened oil storage tank L1 is adopted to supply thickened oil, the hydrogen supply agent storage tank L2 can be communicated with the thickened oil storage tank L1, a hydrogen supply agent is mixed with the thickened oil and then is conveyed to the high-pressure plunger device L4 through the low-pressure feed pump L3, the mixed liquid is pressurized and then is injected into the cavitation treatment device L5, the viscosity of the thickened oil is reduced by using the liquid flow cavitation effect, then the thickened oil after viscosity reduction is injected into the storage tank L6 for storage and standby, and the treated thickened oil can also be collected into the gathering and transportation pipeline L8 for conveying;
when the viscosity reduction system is used as a bypass of a thickened oil gathering and transportation pipeline L8, the gathering and transportation pipeline L8 directly supplies materials to the high-pressure plunger device L4, and the viscosity is reduced by the cavitation treatment device L5 and then stored in a storage tank or directly merged into the gathering and transportation pipeline L8.
Preferably, the cavitation treatment device L5 includes a cavitation nozzle assembly L5-1 and a target plate assembly L5-2, the target plate assembly L5-2 is located at one side of the cavitation nozzle assembly L5-1, and forms a low-speed high-pressure area Q1, a high-speed low-pressure area Q2, an expansion area Q3, and a cavitation collapse area Q4;
thickened oil flows in from cavitation nozzle subassembly L5-1 left side, gets into low-speed high-pressure area Q1, flows out from the right side, gets into high-speed low-pressure area Q2, because of the aperture narrows down, forms the efflux at high-speed low-pressure area Q2 district right side exit, has two low-pressure areas to form around the efflux forms: one is a tangential region Q2-1 when the jet flow is formed, and the other is a vortex region Q2-2 when the jet flow enters a relatively static fluid; the jet flow continues to develop forwards, when the jet flow enters an expansion area Q3, under a certain condition, the pressure of the expansion area Q3 is lower than the necessary pressure required by the stability of gas nuclei, namely the saturated vapor pressure of the liquid at the temperature, the gas nuclei in the liquid grow and rapidly form large cavitation bubbles filled with steam, and after the cavitation bubbles enter a cavitation bubble collapse area Q4, the cavitation bubbles collapse and break due to sudden increase of the pressure or movement to the vicinity of a target plate, so that a cavitation effect is generated;
the collapse of the cavitation bubble generates a very short strong pressure pulse, a tiny space around the bubble generates an extreme high-temperature and high-pressure microenvironment, the local temperature of the microenvironment can reach 1900-5000K, the pressure of the microenvironment exceeds 5 multiplied by 107Pa, and the local temperature is accompanied by strong shock waves and micro jet flow with the speed per hour as high as 400 m/s. Under the extreme environment, under the physical and chemical actions of mechanical shearing, pyrolysis, radical oxidation and supercritical water oxidation, the colloid structure of the thick oil is damaged, colloid and asphaltene macromolecules in the thick oil can generate reactions such as chain scission, cracking and hydrogenation, the macromolecules are changed into micromolecules, the molecular mass is reduced, and the viscosity is reduced.
The thick oil liquid flow cavitation viscosity reduction system provided by the invention has the technical scheme that: comprises a feeding system 2, a control and power system 3, a cavitation processing system 4 and a storage system 5,
the feeding system 2 comprises a hydrogen supply agent storage tank 2-2, a hydrogen supply agent feeding pump 2-3, a tail gas absorption tank 2-4, a stirrer 2-5, a storage tank heater 2-6 and a thick oil storage tank 2-7, wherein the hydrogen supply agent feeding pump 2-3 is arranged at the lower end of the hydrogen supply agent storage tank 2-2 and is connected to the thick oil storage tank 2-7 through a pipeline, the stirrer 2-5 is arranged in the thick oil storage tank 2-7, the tail gas absorption tank 2-4 is arranged at the upper part of the thick oil storage tank 2-7, the stirrer 2-5 is connected and controlled with the power system 3 through control, and the output end of the thick oil storage tank 2-7 is connected to the cavitation treatment system 4 through a pipeline;
the cavitation treatment system 4 comprises a variable frequency motor 4-1, a high-pressure plunger pump 4-2 and a cavitation processor 4-7, wherein the input end of the cavitation processor 4-7 is connected with the high-pressure plunger pump 4-2 and the variable frequency motor 4-1, and the output end of the cavitation processor is connected with a storage system 5;
the storage system 5 comprises a first stirrer 5-1, a second stirrer 5-2, a first product tank 5-3 and a second product tank 5-4, thick oil subjected to cavitation treatment is sent to the first product tank 5-3 or the second product tank 5-4, the first stirrer 5-1 is arranged in the first product tank 5-3, and the second stirrer 5-2 is arranged in the second product tank 5-4.
Preferably, the cavitation processor 4-7 comprises a liquid inlet pipe 4-7-1, a front cover plate 4-7-2, a high-temperature oil-resistant seal 4-7-3, a front end cover 4-7-4, a cavitation nozzle 4-7-5, a reactor cavity 4-7-6, a target plate 4-7-7, a driving nut 4-7-8, a spray distance adjusting rod 4-7-9, an adjusting handle 4-7-10, a rear cover plate 4-7-11, a rear end cover 4-7-12, a bearing 4-7-13, a liquid outlet pipe 4-7-14, a high-pressure tee joint 4-7-15, a sampling port valve 4-7-16, a conveying pipe valve 4-7-17, a conveying pipe 4-7-18, a pull rod 4-7-19 and a fastening nut 4-7-20;
the front end cover 4-7-4 is buckled and pressed in a groove at the right side of the front cover plate 4-7-2 and is arranged at the left side of the reactor cavity 4-7-6; the rear end cover 4-7-12 is buckled and pressed in a groove at the left side of the rear cover plate 4-7-11 and is connected with the right side of the reactor cavity 4-7-6 through threads, and the structures are connected into a closed pressure container through a plurality of pull rods 4-7-19 and fastening nuts 4-7-20; the liquid inlet pipe 4-7-1 is fixed on the front end cover 4-7-4, is spin-connected with the cavitation nozzle 4-7-5 through screw threads, and is placed in a closed pressure vessel; the spray distance adjusting rod 4-7-9 and the driving nut 4-7-8 form a spiral adjusting structure, wherein the left side of the spray distance adjusting rod 4-7-9 is rotatably connected with the target plate 4-7-7, the driving nut 4-7-8 is supported on the right side of the reactor cavity 4-7-6 through a bearing 4-7-13 to form a revolute pair, and the distance between the target plate 4-7-7 and the outlet end of the cavitation nozzle 4-7-5 is adjusted through rotating the adjusting handle 4-7-10; the left side of the reactor cavity 4-7-6 is provided with a liquid outlet pipe 4-7-14, the treated thick oil can be conveyed to a conveying pipe valve 4-7-17 through a high-pressure tee joint 4-7-15 and is conveyed out through a conveying pipe 4-7-18, and in addition, thick oil sampling analysis can be carried out at a sampling port valve 4-7-16.
Preferably, the cavitation nozzle 4-7-5 is composed of a first-stage cavitation nozzle 4-7-5-1, a first-stage transition joint 4-7-5-2, a second-stage cavitation nozzle 4-7-5-3, a second-stage transition joint 4-7-5-4, a third-stage cavitation nozzle 4-7-5-5 and a tail end nozzle 4-7-5-6 which are sequentially connected, and high-temperature oil-resistant seals 4-7-5-7 are respectively arranged, and the cavitation nozzles at all stages and the transition joints at all stages are connected by screwing.
Preferably, the feeding system 2 further comprises a high-pressure four-way 2-1, a pipeline heater 2-12 and a pipeline buffer 2-13, the thick oil is connected with the high-pressure four-way 2-1 through a gathering and transporting pipeline 1, one output end of the high-pressure four-way 2-1 is connected to a thick oil storage tank 2-7 through a pipeline, the other output end of the high-pressure four-way 2-1 is connected to the pipeline heater 2-12 and the pipeline buffer 2-13 through a pipeline, and the output end of the pipeline buffer 2-13 is connected to the cavitation processor 4-7.
Preferably, the inlet cone angle α 1= α 2= α 3=13.5 ° of the primary cavitation nozzle 4-7-5-1, the secondary cavitation nozzle 4-7-5-3, and the tertiary cavitation nozzle 4-7-5-5, and the ratio of the outlet diameters is: d1: d2: d3= 2.
Preferably, the ratio of the outlet diameters of the primary transition joint 4-7-5-2, the secondary transition joint 4-7-5-4 and the end nozzle 4-7-5-6 is: d4: d5: d6= 2; the ratio of the diameter of the outlet of the first-stage cavitation nozzle 4-7-5-1 to the diameter of the inlet of the first-stage transition joint 4-7-5-2 is as follows: d1: d4= 1; the ratio of the diameter of the outlet of the secondary cavitation nozzle 4-7-5-3 to the diameter of the inlet of the secondary transition joint 4-7-5-4 is as follows: d2: d5= 3; the ratio of the outlet diameter of the three-stage cavitation nozzle 4-7-5-5 to the outlet diameter of the tail end nozzle 4-7-5-6 is as follows: d3: d6= 2.
Example 2, the specific method for viscosity reduction by cavitation of thick oil stream provided by the invention comprises the following steps:
(1) Cavitation and viscosity reduction through a gathering and transportation pipeline feeding mode:
referring to fig. 3-10, in the feeding system 2, the stop valve S21, the stop valve S27 and the stop valve S28 are closed, the stop valve S22 is opened, the thick oil enters the high-pressure four-way pipe 2-1 through the gathering and transporting pipeline 1 from the left to the right, flows through the pipeline heater 2-12, the pipeline buffer 2-13 (preventing the thick oil from impacting the flowmeter due to excessive flow velocity) and the flowmeter 2-11, and then enters the cavitation processing system 4 from the B direction, and the check valve T21, the check valve T22 and the check valve T23 can prevent the thick oil from reversely entering the slurry feeding pump 2-8, the first backup slurry feeding pump 2-9 and the second backup slurry feeding pump 2-10; in the cavitation treatment system 4, taking the operation of a single high-pressure plunger pump as an example, opening a stop valve S41, closing a stop valve S42, enabling the thick oil to enter a high-pressure plunger pump 4-2 through the stop valve S41, pressurizing the thick oil by the high-pressure plunger pump 4-2, and displaying the pressure by a pressure gauge 4-5, wherein the pressure is realized by adjusting the rotating speed of a variable frequency motor 4-1 by a control and power system 3; if the pressure of the high-pressure plunger pump 4-2 exceeds the rated pressure, the safety overflow valve Y41 is opened, and the thick oil is injected into the thick oil storage tank 2-7 through the overflow pipeline 4-9; the pressurized thick oil enters a cavitation nozzle 4-7-5 in a cavitation processor 4-7, is modulated by the cavitation nozzle 4-7-5 to form high-speed cavitation jet flow, and then is sprayed out from a tail end nozzle 4-7-5-6, and the viscosity of the thick oil is reduced by utilizing the cavitation effect; the thickened oil after viscosity reduction can enter product tanks 5-3 and 5-4 of a storage system 5 through the C2 direction (at the moment, a stop valve S45 needs to be closed and a stop valve S46 needs to be opened); in addition, the stop valve S46 can be closed, the stop valve S45 can be opened, and the treated thickened oil can be collected into the gathering and transportation pipeline 1 again; in the embodiment, if the hydrogen donor is required to be added into the gathering and transportation pipeline 1, the stop valve S23 is closed, the stop valve S28 is opened, and meanwhile, the hydrogen donor feeding pump 2-3 is started; alternatively, if the high-pressure plunger pump 4-2 fails, the thick oil may be guided to the standby high-pressure plunger pump 4-4, and the specific implementation manner is as follows: closing the stop valve S41, opening the stop valve S42, adjusting the rotating speed of the variable frequency motor 4-3 by the control and power system 3 to adjust the pump pressure, and performing viscosity reduction treatment by the standby cavitation processor 4-8, wherein the treated thick oil enters the first product tank 5-3 and the second product tank 5-4 of the storage system 5 in the direction C1, in the process, if the pressure of the standby high-pressure plunger pump 4-4 exceeds the rated pressure, the safety overflow valve Y42 is opened, and the thick oil is injected into the thick oil storage tank 2-7 through the standby overflow pipeline 4-10.
Example 3, the specific method for cavitation viscosity reduction of thick oil liquid stream provided by the invention comprises the following steps:
(2) Carrying out cavitation viscosity reduction in a thick oil storage tank feeding mode:
referring to fig. 3-10, in a feeding system 2, a stop valve S22 and a stop valve S27 are closed, a stop valve S21 is opened, thick oil enters a high-pressure four-way joint 2-1 from a direction a through a gathering and transportation pipeline 1 from left to right, then flows through the stop valve S21 and enters a thick oil storage tank 2-7, in order to prevent solid particles, water and other impurities in a thick oil mixture from settling (mainly aiming at being directly applied to a thick oil exploitation wellhead), a stirrer 2-5 is opened for stirring, if the thick oil mixture has too low fluidity, a storage tank heater 2-6 is opened for primarily heating and viscosity reduction, so that subsequent transportation is facilitated, and tail gas generated in the heating process enters a tail gas absorption tank 2-4 for treatment; if hydrogen donor needs to be added, starting a hydrogen donor feeding pump 2-3, stirring and mixing the hydrogen donor in the hydrogen donor storage tank 2-2 and the thickened oil in the storage tank 2-7, and at the moment, closing a stop valve S28 and opening a stop valve S23; according to the actual processing capacity and processing rate, the stop valve S24, the stop valve S25 and the stop valve S26 can be selected to be opened completely or opened singly or two, in this embodiment, a single stop valve S24 is opened as an example, and a specific implementation is illustrated, the thick oil mixture enters the slurry feed pump 2-8 through the stop valve S24, the thick oil mixture is pressurized to be at a low pressure in the slurry feed pump 2-8 and then is conveyed to the cavitation processing system 4 through the check valve T21 and the flow meter 2-11 in the direction B, and the check valve T22, the check valve T23 and the check valve T24 can prevent the thick oil from reversely entering the first backup slurry feed pump 2-9, the second backup slurry feed pump 2-10 and the pipeline buffer 2-13; in the cavitation treatment system 4, taking the operation of a single high-pressure plunger pump as an example, opening a stop valve S41, closing a stop valve S42, enabling the thick oil to enter a high-pressure plunger pump 4-2 through the stop valve S41, pressurizing the thick oil by the high-pressure plunger pump 4-2, and displaying the pressure by a pressure gauge 4-5, wherein the pressure is realized by adjusting the rotating speed of a variable frequency motor 4-1 by a control and power system 3; if the pressure of the high-pressure plunger pump 4-2 exceeds the rated pressure, the safety overflow valve Y41 is opened, and the thick oil is injected into the thick oil storage tank 2-7 through the overflow pipeline 4-9; the pressurized thick oil enters a cavitation nozzle 4-7-5 in a cavitation processor 4-7, is modulated by the cavitation nozzle 4-7-5 to form high-speed cavitation jet flow, and then is sprayed out from a tail end nozzle 4-7-5-6, and the viscosity of the thick oil is reduced by utilizing the cavitation effect; the thickened oil after viscosity reduction can enter product tanks 5-3 and 5-4 of a storage system 5 through the C2 direction (at the moment, a stop valve S45 needs to be closed and a stop valve S46 needs to be opened); in addition, the stop valve S46 can be closed, the stop valve S45 can be opened, and the treated thickened oil can be collected into the gathering and transportation pipeline 1 again; in the embodiment, if the hydrogen donor is required to be added into the gathering and transportation pipeline 1, the stop valve S23 is closed, the stop valve S28 is opened, and the hydrogen donor feeding pump 2-3 is started at the same time; alternatively, if the high-pressure plunger pump 4-2 fails, the thick oil may be guided to the standby high-pressure plunger pump 4-4, and the specific implementation manner is as follows: closing the stop valve S41, opening the stop valve S42, adjusting the rotating speed of the variable frequency motor 4-3 by the control and power system 3 to adjust the pump pressure, and performing viscosity reduction treatment by the standby cavitation processor 4-8, wherein the treated thick oil enters the first product tank 5-3 and the second product tank 5-4 of the storage system 5 in the direction C1, in the process, if the pressure of the standby high-pressure plunger pump 4-4 exceeds the rated pressure, the safety overflow valve Y42 is opened, and the thick oil is injected into the thick oil storage tank 2-7 through the standby overflow pipeline 4-10.
Example 4, the specific method for viscosity reduction by cavitation of thick oil stream provided by the invention comprises the following steps:
(3) Non-cavitation viscosity reduction examples
Referring to fig. 3 to 10, if the viscosity of the thick oil in the gathering and transportation pipeline 1 completely meets the gathering and transportation requirement, the thick oil flow cavitation viscosity reduction system can be isolated from the gathering and transportation pipeline 1, and the specific implementation manner is as follows: in the feed system 2, when the stop valves S21 and S22 are closed and the stop valve S27 is opened, the thick oil flows in directly from the left side a and enters the cavitation treatment system 4 from the right side a, and when the stop valves S43 and S45 in the cavitation treatment system 4 are closed, the thick oil flows out directly from the right side without passing through any subsystem in the cavitation treatment system 4.
The specific implementation effects are compared as follows:
1) The method comprises the following steps of performing cavitation viscosity reduction by adopting a thick oil storage tank feeding mode, adding no hydrogen donor, primarily heating raw oil in a storage tank 2-7 to 60 ℃ by a storage tank heater 2-6, and respectively controlling the working pressure of a high-pressure plunger pump 4-2 to be 20MPa, 30MPa and 42MPa, wherein the implementation effect is as follows:
2) Performing cavitation viscosity reduction by adopting a thick oil storage tank feeding mode, taking thick oil of 'Shengli oilfield Hei 2-well' as a processing object, respectively adding water and tetrahydronaphthalene as hydrogen supply agents, preliminarily heating a thick oil mixture in a storage tank 2-7 to 60 ℃ by a storage tank heater 2-6, and performing high-pressure plunger pump 4-2 under the working pressure of 30MPa, wherein the implementation effect is as follows:
from the above examples it can be seen that:
(1) under the working condition that no hydrogen donor is added, the viscosity reduction rate of the treated thickened oil can respectively reach more than 70 percent and more than 85 percent;
(2) the viscosity reduction rate of the marine heavy oil is about 40 percent and more than 15 percent respectively;
(3) the viscosity of the raw oil before treatment is higher, and the viscosity reduction rate after cavitation viscosity reduction treatment is higher;
(4) the larger the pump pressure is, the better the cavitation viscosity reduction effect is;
(5) the viscosity recovery rate of the treated heavy oil and heavy oil after standing for 10 days is very small;
(6) the viscosity reduction rate is further increased when the hydrogen donor is added, and the effect of the tetrahydronaphthalene is obviously better than that of water.
The system not only can be used for viscosity reduction and gathering of thick oil, crude oil pretreatment in an oil refinery, crude oil pretreatment at a thick oil extraction well mouth and the like in the field of petroleum development, but also can be integrated into large ships using heavy oil as fuel, such as ocean oil tankers, conventional power aircraft carriers and the like as an auxiliary system of a power core cabin, so that the preheating time of a main engine is shortened; in addition, the cavitation nozzle assembly can be formed by connecting one or more cavitation nozzles in series or in parallel, and the flow channel of the cavitation nozzle can be replaced by an angle type nozzle, a Helmholtz nozzle, an organ pipe self-vibration cavitation nozzle, a central body cavitation nozzle, an orifice plate type cavitation nozzle and the like
The above description is only a few of the preferred embodiments of the present invention, and any person skilled in the art may modify the above-described embodiments or modify them into equivalent ones. Therefore, the technical solution according to the present invention is subject to corresponding simple modifications or equivalent changes, as far as the scope of the present invention is claimed.
Claims (7)
1. A thick oil liquid flow cavitation viscosity reduction process method is characterized in that: the device comprises a thickened oil storage tank (L1), a hydrogen supply agent storage tank (L2), a low-pressure feed pump (L3), a high-pressure plunger device (L4), a cavitation treatment device (L5), a thickened oil injection storage tank (L6) and a thickened oil gathering and transportation pipeline (L8), wherein when the thickened oil storage tank (L1) is used for supplying thickened oil, the hydrogen supply agent storage tank (L2) is communicated with the thickened oil storage tank (L1), the hydrogen supply agent and the thickened oil are mixed and then are conveyed to the high-pressure plunger device (L4) through the low-pressure feed pump (L3), mixed liquid is pressurized and then injected into the cavitation treatment device (L5), the viscosity of the thickened oil is reduced by using a liquid flow cavitation effect, the thickened oil after viscosity reduction is injected into the storage tank (L6) for storage and standby, and the treated thickened oil is gathered into the gathering and transportation pipeline (L8) for conveying;
when the viscosity reduction system is used as a side branch of a thick oil gathering and transportation pipeline (L8), the gathering and transportation pipeline (L8) directly supplies materials to the high-pressure plunger device (L4), and the viscosity is reduced by the cavitation treatment device (L5) and then stored in the storage tank or directly merged into the gathering and transportation pipeline (L8);
the cavitation treatment device (L5) comprises a cavitation nozzle component (L5-1) and a target plate component (L5-2), wherein the target plate component (L5-2) is positioned on one side of the cavitation nozzle component (L5-1) and forms a low-speed high-pressure area (Q1), a high-speed low-pressure area (Q2), an expansion area (Q3) and a cavitation collapse area (Q4);
thickened oil flows in from cavitation nozzle subassembly (L5-1) left side, gets into low-speed high-pressure area (Q1), flows out from the right side, gets into high-speed low-pressure area (Q2), because of the aperture narrows, forms the efflux at high-speed low-pressure area (Q2) district right side exit, has two low-pressure areas to form around the efflux formation: one is a tangential region (Q2-1) when the jet is formed, and the other is a vortex region (Q2-2) when the jet enters a relatively static fluid; the jet flow continues to develop forwards and enters an expansion area (Q3), the pressure of the expansion area (Q3) is lower than the necessary pressure required by the gas nucleus stabilization, namely the saturated vapor pressure of the liquid at the temperature, the gas nucleus in the liquid grows and rapidly forms large cavitation bubbles filled with steam, and after the cavitation bubbles enter a cavitation bubble collapse area (Q4), the cavitation bubbles collapse and collapse due to the sudden increase of the pressure or the movement of the cavitation bubbles to the vicinity of a target plate, so that a cavitation effect is generated;
the collapse of the cavitation bubble can generate very transient strong pressure pulse, the micro space around the bubble can generate extreme high temperature and high pressure micro environment, the local temperature can reach 1900-5000K, the pressure can exceed 5 x 107Pa, and the strong shock wave and the micro jet flow with the speed per hour as high as 400m/s are accompanied; under the extreme environment, under the physical and chemical actions of mechanical shearing, pyrolysis, radical oxidation and supercritical water oxidation, the colloid structure of the thick oil is damaged, the colloid and asphaltene macromolecules in the thick oil can undergo chain scission, cracking and hydrogenation reactions, the macromolecules are changed into micromolecules, the molecular mass is reduced, and the viscosity is reduced.
2. The thick oil stream cavitation viscosity reduction process method as set forth in claim 1, which is characterized in that: comprises a feeding system (2), a control and power system (3), a cavitation treatment system (4) and a storage system (5),
the feeding system (2) comprises a hydrogen supply agent storage tank (L2), a hydrogen supply agent feeding pump (2-3), a tail gas absorption tank (2-4), a stirrer (2-5), a storage tank heater (2-6) and a thick oil storage tank (L1), wherein the hydrogen supply agent feeding pump (2-3) is arranged at the lower end of the hydrogen supply agent storage tank (L2) and is connected to the thick oil storage tank (L1) through a pipeline, the stirrer (2-5) is arranged in the thick oil storage tank (L1), the tail gas absorption tank (2-4) is arranged at the upper part of the thick oil storage tank (L1), the stirrer (2-5) is connected and controlled with the power system (3) through control, and the output end of the thick oil storage tank (L1) is connected to the cavitation treatment system (4) through a pipeline;
the cavitation treatment system (4) comprises a variable frequency motor (4-1), a high-pressure plunger pump (4-2) and a cavitation processor (4-7), the input end of the cavitation processor (4-7) is connected with the high-pressure plunger pump (4-2) and the variable frequency motor (4-1), and the output end of the cavitation processor is connected with the storage system (5);
the storage system (5) comprises a first stirrer (5-1), a second stirrer (5-2), a first product tank (5-3) and a second product tank (5-4), thick oil subjected to cavitation treatment is sent to the first product tank (5-3) or the second product tank (5-4), the first stirrer (5-1) is arranged in the first product tank (5-3), and the second stirrer (5-2) is arranged in the second product tank (5-4).
3. The thick oil stream cavitation viscosity reduction process method as set forth in claim 2, characterized in that: the cavitation processor (4-7) comprises a liquid inlet pipe (4-7-1), a front cover plate (4-7-2), a high-temperature oil-resistant seal (4-7-3), a front end cover (4-7-4), a cavitation nozzle (4-7-5), a reactor cavity (4-7-6), a target plate (4-7-7), a driving nut (4-7-8), a spray distance adjusting rod (4-7-9), an adjusting handle (4-7-10), a rear cover plate (4-7-11), a rear end cover (4-7-12), a bearing (4-7-13), a liquid outlet pipe (4-7-14), a high-pressure tee joint (4-7-15), a sampling port valve (4-7-16), a delivery pipe valve (4-7-17), a delivery pipe (4-7-18), a pull rod (4-7-19) and a fastening nut (4-7-20);
the front end cover (4-7-4) is buckled and pressed in a groove at the right side of the front cover plate (4-7-2) and is arranged at the left side of the reactor cavity (4-7-6) at the same time; the rear end cover (4-7-12) is buckled and pressed in a groove at the left side of the rear cover plate (4-7-11) and is connected with the right side of the reactor cavity (4-7-6) through threads, and the structure is connected into a closed pressure container through a plurality of pull rods (4-7-19) and fastening nuts (4-7-20); the liquid inlet pipe (4-7-1) is fixed on the front end cover (4-7-4), is spirally connected with the cavitation nozzle (4-7-5) through threads, and is placed in a closed pressure vessel; the spray distance adjusting rod (4-7-9) and the driving nut (4-7-8) form a spiral adjusting structure, wherein the left side of the spray distance adjusting rod (4-7-9) is connected with the target plate (4-7-7) in a screwing manner, the driving nut (4-7-8) is supported on the right side of the reactor cavity (4-7-6) through a bearing (4-7-13) to form a revolute pair, and the distance between the target plate (4-7-7) and the outlet end of the cavitation nozzle (4-7-5) is adjusted through rotating the adjusting handle (4-7-10); a liquid outlet pipe (4-7-14) is arranged on the left side of the reactor cavity (4-7-6), the treated thick oil is conveyed to a conveying pipe valve (4-7-17) through a high-pressure tee joint (4-7-15), the thick oil is conveyed out through a conveying pipe (4-7-18), and thick oil sampling analysis is carried out at a sampling port valve (4-7-16).
4. The thick oil stream cavitation viscosity reduction process method as set forth in claim 3, characterized in that: the cavitation nozzle (4-7-5) is formed by sequentially connecting a first-stage cavitation nozzle (4-7-5-1), a first-stage transition joint (4-7-5-2), a second-stage cavitation nozzle (4-7-5-3), a second-stage transition joint (4-7-5-4), a third-stage cavitation nozzle (4-7-5-5) and a tail end nozzle (4-7-5-6), and is respectively provided with a cavitation nozzle high-temperature oil-resistant seal (4-7-5-7), and the cavitation nozzles at all stages are connected with the transition joints at all stages through thread spinning.
5. The thick oil stream cavitation viscosity reduction process method as set forth in claim 2, characterized in that: the feeding system (2) further comprises a high-pressure four-way joint (2-1), a pipeline heater (2-12) and a pipeline buffer (2-13), thick oil is connected with the high-pressure four-way joint (2-1) through a gathering and transporting pipeline (L8), one output end of the high-pressure four-way joint (2-1) is connected to the thick oil storage tank (L1) through a pipeline, the other output end of the high-pressure four-way joint (2-1) is connected to the pipeline heater (2-12) and the pipeline buffer (2-13) through a pipeline, and the output end of the pipeline buffer (2-13) is connected to the cavitation processor (4-7).
6. The thick oil stream cavitation viscosity reduction process of claim 4, which is characterized in that: the inlet cone angle alpha 1= alpha 2= alpha 3=13.5 ° of the primary cavitation nozzle (4-7-5-1), the secondary cavitation nozzle (4-7-5-3) and the tertiary cavitation nozzle (4-7-5-5), and the ratio of the outlet diameters is as follows: d1: d2: d3= 2.
7. The thick oil stream cavitation viscosity reduction process of claim 6, which is characterized in that: the ratio of the outlet diameters of the primary transition joint (4-7-5-2), the secondary transition joint (4-7-5-4) and the tail end nozzle (4-7-5-6) is as follows: d4: d5: d6= 2; the ratio of the diameter of the outlet of the first-stage cavitation nozzle (4-7-5-1) to the diameter of the inlet of the first-stage transition joint (4-7-5-2) is as follows: d1: d4= 1; the ratio of the diameter of the outlet of the secondary cavitation nozzle (4-7-5-3) to the diameter of the inlet of the secondary transition joint (4-7-5-4) is as follows: d2: d5= 3; the ratio of the diameter of the outlet of the three-stage cavitation nozzle (4-7-5-5) to the diameter of the outlet of the tail end nozzle (4-7-5-6) is as follows: d3: d6= 2.
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| CN205412938U (en) * | 2016-03-29 | 2016-08-03 | 中国石油大学(华东) | Heavy oil hydrogen supply inferior subtracts and glues cracking analogue means |
| CN107674700A (en) * | 2017-10-17 | 2018-02-09 | 中石化炼化工程（集团）股份有限公司 | Heavy oil low temperature lightening method and heavy oil low temperature lighting system and application |
| CN110591758A (en) * | 2019-09-29 | 2019-12-20 | 中国石油化工股份有限公司 | Pretreatment method of residual oil hydrogenation raw material and residual oil hydrogenation method |
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| EP2751225A4 (en) * | 2011-09-14 | 2015-05-06 | Arisdyne Systems Inc | Method for processing heavy hydrocarbon oil |
| US20150315494A1 (en) * | 2014-05-01 | 2015-11-05 | Exxonmobil Research And Engineering Company | Methods and systems for improving the properties of products of a heavy feed steam cracker |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN205412938U (en) * | 2016-03-29 | 2016-08-03 | 中国石油大学(华东) | Heavy oil hydrogen supply inferior subtracts and glues cracking analogue means |
| CN107674700A (en) * | 2017-10-17 | 2018-02-09 | 中石化炼化工程（集团）股份有限公司 | Heavy oil low temperature lightening method and heavy oil low temperature lighting system and application |
| CN110591758A (en) * | 2019-09-29 | 2019-12-20 | 中国石油化工股份有限公司 | Pretreatment method of residual oil hydrogenation raw material and residual oil hydrogenation method |
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