CN113862032A - Method for treating thickened oil by supercritical water and supersonic separator together - Google Patents
Method for treating thickened oil by supercritical water and supersonic separator together Download PDFInfo
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- CN113862032A CN113862032A CN202111064536.6A CN202111064536A CN113862032A CN 113862032 A CN113862032 A CN 113862032A CN 202111064536 A CN202111064536 A CN 202111064536A CN 113862032 A CN113862032 A CN 113862032A
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
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Abstract
The invention relates to a method for treating thickened oil by supercritical water and a supersonic speed separator, which comprises the steps of respectively heating and pressurizing thickened oil and deionized water, mixing oil with water, heating and conveying to a supercritical water reactor, and performing pyrolysis reaction on the thickened oil in the supercritical water reactor by utilizing a supercritical water thermal thickened oil modification technology to realize light-weight conversion of the thickened oil. After the thickened oil is modified, the phase state and the dissolution characteristic of water are changed by utilizing the temperature and the pressure reduction of a supersonic separator, so that the separation of light and heavy components is realized, the separated heavy component asphaltene forms asphalt solid particles through a granulation tower, and the separation of pyrolysis gas, light oil and wastewater is realized by reducing the temperature and the pressure of the light component. The method not only realizes the rapid reaction of supercritical hydrothermal modified thick oil and greatly realizes the light-weight conversion of the thick oil, but also realizes the rapid separation of light and heavy components of the modified oil by using the supersonic separator, and the whole process is simple and efficient.
Description
Technical Field
The invention relates to the field of thickened oil modification, in particular to a thickened oil modification method utilizing supercritical water thermal cracking and supersonic separator technology.
Background
The thickened oil is an unconventional petroleum resource and has abundant geological reserves. The thick oil features high viscosity, density and solidifying point, and high content of asphaltine, so it is a poor crude oil difficult to process and utilize.
Research shows that the supercritical water modified thickened oil has better viscosity reduction and lightening effects. Compared with the thermal cracking reaction of the thickened oil, the supercritical water has particularly strong heat conductivity, fluidity and heat conductivity, and has the function of inhibiting coke formation when the thickened oil is modified by the supercritical water. After the thick oil is subjected to hydrothermal treatment, the thick oil generally needs to undergo the procedures of oil-water separation, solvent deasphalting and solvent recovery, and the process has energy waste and is complex.
At present, there are patents disclosing apparatuses and processes for reactions using supercritical water.
Patent CN101077980A adds vacuum residue and water into a high-pressure autoclave with stirring, and after heating and pressurizing reaction and cooling, light oil is obtained, or the light oil is put into a static tubular reactor, after temperature control reaction in a molten salt furnace, the light oil is obtained by quenching in a water tank, and the reactor is cleaned by n-heptane to obtain the target product.
Patent CN102676205A proposes introducing a radical initiator to improve the thermal cracking of heavy oil in subcritical water, wherein the radical initiator is selected from one or more of elementary iodine, peroxide initiators and azo initiators, and the radical initiator is used for stabilizing the excessively high reaction temperature threshold of the thermal cracking of the heavy oil in the induction period, so that the thermal cracking of the heavy oil can be carried out under the mild condition, coking is effectively inhibited while the distribution of cracked liquid phase products is improved, the introduction of the radical initiator increases the process cost, and some difficulties are brought to the subsequent treatment of the modified thick oil.
Patent CN103013550A discloses a system and a method for preparing fuel oil by modifying tar residue with supercritical water, wherein a material and an oxygen source are respectively conveyed into a supercritical water reactor, and a heating device in the reactor is started to carry out modification reaction on tar residue in the supercritical water. The invention can realize the resource utilization of the tar residue, the temperature of the mixed material of the tar residue and water needs to be raised by hundreds of degrees after the mixed material is input into the reactor, the heating time is long, the treatment capacity of the system is low, meanwhile, the local temperature near the heating device is overhigh, the tar residue is easy to generate coke, and the internal space of the reactor is blocked.
Patent CN106170532A discloses a method for upgrading petroleum feedstock using a supercritical water petroleum upgrading system, combining petroleum feedstock and water to form a mixed petroleum feedstock, and introducing the mixed petroleum feedstock and water into the lower part of an upflowing supercritical water reactor simultaneously, respectively. One embodiment of the method includes operating the supercritical water petroleum upgrading system that includes an upflowing supercritical water reactor and optionally a downflowing supercritical water reactor to introduce upflowing reactor product fluid into the upper portion of the downflowing supercritical water reactor. The method increases the temperature in the reactor, can increase the upgrading effect to a certain extent, but the increase of the temperature also increases the coke formation amount and increases the risk of blocking pipelines and the reactor.
Patent CN106987265A discloses mixing heavy oil in supercritical water environment with preset thermodynamic state to form a mixed phase, and performing thermal cracking reaction of the heavy oil in the mixed phase, wherein the thermal cracking reaction of the heavy oil is selectively performed toward dealkylation by the diffusion environment in the mixed phase and the activation of the supercritical water on the carbocation of the aromatic side chain olefin end group.
Disclosure of Invention
The technical problem to be solved by the invention is to overcome the defects in the prior art, and provide a method for modifying thickened oil by supercritical water, and then reducing the temperature and pressure by a supersonic separator to change the solubility of oil and water, so as to realize the separation of pyrolysis gas, light oil, wastewater and asphaltene.
The invention relates to a method for treating thick oil by supercritical water and a supersonic separator, which comprises the following treatment steps:
1) respectively heating a deionized water flow and a thick oil to 50-90 ℃, pressurizing to 22.1-30 MPa, conveying to an inlet of a mixer, wherein the mass flow ratio of the thick oil to the deionized water flow is 0.2-4, mixing the thick oil and the deionized water in the mixer to obtain an oil-water mixed solution, heating the oil-water mixed solution to 400-500 ℃, and conveying to an inlet of a primary supercritical water reactor;
2) the thickened oil is subjected to pyrolysis reaction in a first-stage supercritical water reactor and a second-stage supercritical water reactor in sequence, the residence time of the thickened oil in the first-stage supercritical water reactor is 1 s-5 min, the residence time of the thickened oil in the second-stage supercritical water reactor is 5 s-10 min, and a mixed fluid of supercritical water, modified thickened oil and pyrolysis gas generated by reaction is discharged from an upper outlet of the second-stage supercritical water reactor;
3) the mixed fluid in the step 2) enters from an inlet of the supersonic separator, a swirl generator in the supersonic separator generates a rotating flow field, then the mixed fluid passes through a spray pipe in the supersonic separator, the axial speed and the tangential speed are increased, the temperature and the pressure are respectively lower than the critical temperature and the critical pressure of water, heavy components rich in asphaltene are separated out from a water-oil mutual solution system, droplets of the separated heavy components continuously collide and coalesce into condensed liquid in the rotating flow field, the condensed liquid is thrown to the wall surface under the centrifugal action and continuously flows under the driving of an air flow, at a separation section, the condensed liquid is driven by the air flow and is discharged from a liquid phase outlet, the temperature of the liquid phase outlet is 330-370 ℃, the pressure of the liquid phase outlet is 12-16 MPa, the air flow is recovered by a diffuser and is discharged from a gas phase outlet, the pressure of the gas phase outlet is 14-18 MPa, the temperature of the gas phase outlet is 350-390 ℃;
4) cooling the airflow discharged from the gas phase outlet in the step 3) to 30-100 ℃, reducing the pressure to 0.1-0.5 MPa, transmitting the airflow into an oil-water separator, separating the airflow into pyrolysis gas, light product oil and wastewater, transmitting the condensate discharged from the liquid phase outlet in the step 3) into a granulation tower, controlling the operation pressure of the granulation tower to be 5-20 MPa and the operation temperature to be 40-120 ℃, and spraying the condensate through a nozzle and dispersing the condensate into solid particles rich in asphaltene.
In the method for treating the thick oil by using the supercritical water and the supersonic separator, preferably, the pressure of the deionized water and the pressure of the thick oil after pressurization in the step 1) are both 22.1-25 MPa.
In the method for treating the thick oil by using the supercritical water and the supersonic separator, the mass flow ratio of the thick oil and the deionized water flow in the step 1) is preferably 1-2.
In the method for treating thick oil by using supercritical water and a supersonic separator, the temperature of the oil-water mixed solution in the step 1) after being heated is preferably 400-450 ℃.
In the above method for treating heavy oil by using supercritical water and supersonic separator together, preferably, the first-stage supercritical water reactor and the second-stage supercritical water reactor in step 2) are vertical tube type upflow reactors, and the diameter of the second-stage supercritical water reactor is 1.5-3 times that of the first-stage supercritical water reactor.
In the method for treating the thick oil by using the supercritical water and the supersonic separator, preferably, the residence time of the thick oil in the first-stage supercritical water reactor in the step 2) is preferably 1-2 min, and the residence time of the thick oil in the second-stage supercritical water reactor is preferably 1-4 min.
In the method for treating thick oil by using supercritical water and a supersonic separator, preferably, the temperature of the cooled gas flow discharged from the gas phase outlet in the step 4) is 50-80 ℃.
In the method for treating thick oil by using supercritical water and a supersonic separator, preferably, the pressure of the gas flow discharged from the gas phase outlet in the step 4) after depressurization is 0.1-0.2 MPa.
In the method for treating the thick oil by using the supercritical water and the supersonic separator, the operation pressure of the prilling tower in the step 4) is preferably 10-16 MPa.
In the method for treating the thick oil by using the supercritical water and the supersonic speed separator, the operation temperature of the prilling tower in the step 4) is preferably 50-100 ℃.
The method combines the supercritical water reactor with the supersonic separator, thereby realizing the rapid reaction of supercritical water modified thickened oil, greatly realizing the light transformation of thickened oil, realizing the rapid separation of light and heavy components through the temperature and pressure reduction characteristic of the supersonic separator, leading the asphaltene to form solid particles through the granulation tower, and utilizing the oil-water separator to realize the separation of pyrolysis gas, wastewater and light oil.
Drawings
FIG. 1 is a schematic diagram of a method for treating thick oil by using supercritical water and a supersonic separator together according to the present invention.
Description of the reference numerals
1 is a water heater, 2 is a water booster pump, 3 is a thickened oil heater, 4 is an oil booster pump, 5 is a mixer, 6 is a heater, 7 is a primary supercritical water reactor, 8 is a secondary supercritical water reactor, 9 is a supersonic separator, 10 is a high-pressure air cooler, 11 is a back pressure valve, 12 is an oil-water separator, and 13 is a prilling tower.
101 is deionized water flow, 102 is thick oil, 103 is asphalt particles, 104 is light product oil, 105 is waste water, and 106 is pyrolysis gas.
Detailed Description
The invention relates to a method for treating thick oil by supercritical water and a supersonic separator, which comprises the following treatment steps:
1) respectively heating the deionized water flow and the thick oil to 50-90 ℃, pressurizing to 22.1-30 MPa (preferably 22.1-25 MPa), and conveying to an inlet of a mixer, wherein the mass flow ratio of the thick oil to the deionized water flow is 0.2-4, preferably 1-2; mixing the thickened oil and deionized water in a mixer to obtain an oil-water mixed solution, heating the oil-water mixed solution to 400-500 ℃, preferably adding the oil-water mixed solution to 400-450 ℃, and then conveying the oil-water mixed solution to an inlet of a primary supercritical water reactor;
2) the thick oil is subjected to pyrolysis reaction in a first-stage supercritical water reactor and a second-stage supercritical water reactor in sequence, and mixed fluid of supercritical water, the modified thick oil and pyrolysis gas generated by the reaction is discharged from an upper outlet of the second-stage supercritical water reactor; wherein the residence time of the thickened oil in the first-stage supercritical water reactor is 1 s-5 min, and the preferred residence time is 1-2 min; the residence time of the thickened oil in the secondary supercritical water reactor is 5 s-10 min, and the preferred residence time is 1-4 min;
3) the mixed fluid in the step 2) enters from the inlet of the supersonic separator, a swirl generator in the supersonic separator generates a rotating flow field, then the mixed fluid passes through a spray pipe in the supersonic separator, the axial speed and the tangential speed are increased, the temperature and the pressure are respectively lower than the critical temperature and the pressure of water, heavy components rich in asphaltene are separated out from a water-oil miscible system, in the rotating flow field, the separated heavy component droplets continuously collide and coalesce into condensate, are thrown to the wall surface under the centrifugal action and continuously flow under the drive of air flow, at the separation section, the condensate is driven by the air flow to be discharged from a liquid phase outlet, the temperature of the liquid phase outlet is 330-370 ℃, the pressure of the liquid phase outlet is 12-16 MPa, after the pressure of the air flow is recovered by a diffuser, discharging from a gas phase outlet, wherein the pressure of the gas phase outlet is 14-18 MPa, and the temperature of the gas phase outlet is 350-390 ℃;
4) cooling the gas flow discharged from the gas phase outlet in the step 3) to 30-100 ℃, reducing the pressure to 0.1-0.5 MPa (preferably, the temperature after cooling the gas flow is 50-80 ℃, and the pressure after reducing the pressure is 0.1-0.2 MPa), transferring the gas flow into an oil-water separator, separating the gas flow into pyrolysis gas, light product oil and waste water, conveying the condensate discharged from the liquid phase outlet in the step 3) into a granulation tower, and spraying the condensate through a nozzle and dispersing the condensate into solid particles rich in asphaltene; wherein the operating pressure of the granulation tower is 5-20 MPa, the operating temperature is controlled at 40-120 ℃, preferably 10-16 MPa, and the operating temperature is controlled at 50-100 ℃.
In the above method for treating heavy oil by using supercritical water and supersonic separator together, preferably, the first-stage supercritical water reactor and the second-stage supercritical water reactor in step 2) are vertical tube type upflow reactors, and the diameter of the second-stage supercritical water reactor is 1.5-3 times that of the first-stage supercritical water reactor.
The present invention will be further described in the following detailed description with reference to the drawings, but the invention is not limited thereto.
As shown in figure 1, deionized water flow 101 is heated to 50-90 ℃ by a water heater 1, pressurized to 22.1-30 MPa by a water booster pump 2 and then conveyed to an inlet of a mixer 5. The thick oil 102 is heated to 50-90 ℃ by a thick oil heater 3, pressurized to 22.1-30 MPa by an oil booster pump 4 and then conveyed to the inlet of a mixer 5. The mass flow of the thickened oil is 0.2-4 times of the mass flow of the deionized water. Mixing the thickened oil and the deionized water in the mixer 5 to obtain an oil-water mixed solution, heating the oil-water mixed solution to 400-500 ℃ by the heater 6, and then conveying the oil-water mixed solution to the inlet of the primary supercritical water reactor 7. The thick oil is subjected to pyrolysis reaction in a first-stage supercritical water reactor 7 and a second-stage supercritical water reactor 8 in sequence, the residence time of the thick oil in the first-stage supercritical water reactor 7 is 1 s-5 min, the residence time in the second-stage supercritical water reactor 8 is 5 s-10 min, and a mixed fluid of supercritical water, the modified thick oil and pyrolysis gas generated by reaction is discharged from an upper outlet of the second-stage supercritical water reactor 8 and is transmitted to a supersonic separator 9 to be separated into a liquid phase rich in asphaltene heavy components and a gas phase rich in light components. The liquid phase rich in asphaltene is used for producing asphalt particles 103 through a granulation tower 13, the gas phase of the light component is cooled to 30-100 ℃ through a high-pressure air cooler 10, is reduced to 0.1-0.5 MPa through a back pressure valve 11, and is conveyed to an oil-water separator 12 to be separated into pyrolysis gas 106, light product oil 104 and waste water 105.
The present invention will be described in detail below by way of examples, but the present invention is not limited thereto.
Example 1
This example is used to illustrate the method for treating thick oil by supercritical water and supersonic separator provided by the present invention.
On a supercritical water heavy oil modifying device provided with a two-stage upflow supercritical water reactor, the inner diameter of a first-stage vertical pipe type supercritical water reactor is 12mm, the height of the first-stage vertical pipe type supercritical water reactor is 4m, and the inner diameter of a second-stage vertical pipe type supercritical water reactor is 20mm, and the height of the second-stage vertical pipe type supercritical water reactor is 4 m.
The mass flow of the deionized water is 14kg/h, the deionized water is heated to 60 ℃, and the pressure is increased to 23MPa through a diaphragm pump. Oil sand asphalt is used as a raw material, the properties of thick oil are shown in table 1, the mass flow rate of the thick oil is 7kg/h, the thick oil raw material is heated to 60 ℃, the pressure is increased to 23MPa through a diaphragm pump, an oil-water mixed solution is heated to 400 ℃ through a heater, and the oil-water mixed solution is conveyed to an inlet of a first-stage supercritical water reactor. The thick oil is subjected to pyrolysis reaction in a first-stage supercritical water reactor and a second-stage supercritical water reactor in sequence, the residence time of the thick oil in the first-stage supercritical water reactor is 1.3min, the residence time of the thick oil in the second-stage supercritical water reactor is 3.6min, a mixture of supercritical water, the modified thick oil and pyrolysis gas generated by reaction is discharged from an upper outlet of the second-stage supercritical water reactor, the mixture is cooled, depressurized and separated by a supersonic separator, and the separated heavy component liquid phase is transmitted to a granulation tower to produce asphalt particles. The light component gas phase is cooled by a high-pressure air cooler, is reduced in pressure by a back pressure valve and is transmitted to an oil-water separator to be separated into pyrolysis gas, light product oil and wastewater. The yield of each component can be calculated by detecting the product. The product analysis results are shown in tables 3 and 4.
Example 2
This example is used to illustrate the method for treating thick oil by supercritical water and supersonic separator provided by the present invention.
On a supercritical water heavy oil modifying device provided with a two-stage upflow supercritical water reactor, the inner diameter of a first-stage vertical pipe type supercritical water reactor is 12mm, the height of the first-stage vertical pipe type supercritical water reactor is 4m, and the inner diameter of a second-stage vertical pipe type supercritical water reactor is 20mm, and the height of the second-stage vertical pipe type supercritical water reactor is 4 m.
The mass flow of the deionized water is 14kg/h, the deionized water is heated to 70 ℃, and the pressure is increased to 23MPa through a diaphragm pump. Oil sand asphalt raw material, the properties of thick oil are shown in table 1, the mass flow rate of the thick oil is 7kg/h, the thick oil raw material is heated to 70 ℃, the thick oil raw material is pressurized to 23MPa by a diaphragm pump, oil-water mixed liquid is heated to 420 ℃ by a heater, and the oil-water mixed liquid is conveyed to the inlet of a first-stage supercritical water reactor. The thick oil is subjected to pyrolysis reaction in a first-stage supercritical water reactor and a second-stage supercritical water reactor in sequence, the residence time of the thick oil in the first-stage supercritical water reactor is 1.3min, the residence time of the thick oil in the second-stage supercritical water reactor is 3.6min, a mixture of supercritical water, the modified thick oil and pyrolysis gas generated by reaction is discharged from an upper outlet of the second-stage supercritical water reactor, the mixture is cooled, depressurized and separated by a supersonic separator, and the separated heavy component liquid phase is transmitted to a granulation tower to produce asphalt particles. The light component gas phase is cooled by a high-pressure air cooler, is reduced in pressure by a back pressure valve and is transmitted to an oil-water separator to be separated into pyrolysis gas, light product oil and wastewater. The yield of each component can be calculated by detecting the product. The product analysis results are shown in tables 3 and 4.
Example 3
This example is used to illustrate the method for treating thick oil by supercritical water and supersonic separator provided by the present invention.
On a supercritical water heavy oil modifying device provided with a two-stage upflow supercritical water reactor, the inner diameter of a first-stage vertical pipe type supercritical water reactor is 12mm, the height of the first-stage vertical pipe type supercritical water reactor is 4m, and the inner diameter of a second-stage vertical pipe type supercritical water reactor is 20mm, and the height of the second-stage vertical pipe type supercritical water reactor is 4 m.
The mass flow of the deionized water is 20kg/h, the deionized water is heated to 80 ℃, and the pressure is increased to 25MPa through a diaphragm pump. Oil sand asphalt is used as a raw material, the properties of thick oil are shown in table 1, the mass flow rate of the thick oil is 30kg/h, the thick oil raw material is heated to 70 ℃, the thick oil raw material is pressurized to 25MPa by a diaphragm pump, an oil-water mixed solution is heated to 450 ℃ by a heater and is conveyed to the inlet of a first-stage supercritical water reactor. The thick oil is subjected to pyrolysis reaction in a first-stage supercritical water reactor and a second-stage supercritical water reactor in sequence, the residence time of the thick oil in the first-stage supercritical water reactor is 0.5min, the residence time of the thick oil in the second-stage supercritical water reactor is 1.5min, a mixture of supercritical water, the modified thick oil and pyrolysis gas generated by reaction is discharged from an upper outlet of the second-stage supercritical water reactor, the mixture is cooled, depressurized and separated by a supersonic separator, and the separated heavy component liquid phase is transmitted to a granulation tower to produce asphalt particles. The light component gas phase is cooled by a high-pressure air cooler, is reduced in pressure by a back pressure valve and is transmitted to an oil-water separator to be separated into pyrolysis gas, light product oil and wastewater. The yield of each component can be calculated by detecting the product. The product analysis results are shown in tables 3 and 4.
Example 4
This example is used to illustrate the method for treating thick oil by supercritical water and supersonic separator provided by the present invention.
On a supercritical water heavy oil modifying device provided with a two-stage upflow supercritical water reactor, the inner diameter of a first-stage vertical pipe type supercritical water reactor is 12mm, the height of the first-stage vertical pipe type supercritical water reactor is 4m, and the inner diameter of a second-stage vertical pipe type supercritical water reactor is 20mm, and the height of the second-stage vertical pipe type supercritical water reactor is 4 m.
The mass flow of the deionized water is 20kg/h, the deionized water is heated to 70 ℃, and the pressure is increased to 25MPa through a diaphragm pump. Oil sand asphalt is used as a raw material, the properties of thick oil are shown in table 1, the mass flow rate of the thick oil is 20kg/h, the thick oil raw material is heated to 70 ℃, the thick oil raw material is pressurized to 25MPa by a diaphragm pump, an oil-water mixed solution is heated to 410 ℃ by a heater and is conveyed to the inlet of a first-stage supercritical water reactor. The thick oil is subjected to pyrolysis reaction in a first-stage supercritical water reactor and a second-stage supercritical water reactor in sequence, the residence time of the thick oil in the first-stage supercritical water reactor is 0.7min, the residence time of the thick oil in the second-stage supercritical water reactor is 1.9min, a mixture of supercritical water, the modified thick oil and pyrolysis gas generated by reaction is discharged from an upper outlet of the second-stage supercritical water reactor, the mixture is cooled, depressurized and separated by a supersonic separator, and the separated heavy component liquid phase is transmitted to a granulation tower to produce asphalt particles. The light component gas phase is cooled by a high-pressure air cooler, is reduced in pressure by a back pressure valve and is transmitted to an oil-water separator to be separated into pyrolysis gas, light product oil and wastewater. The yield of each component can be calculated by detecting the product. The product analysis results are shown in tables 3 and 4.
TABLE 1 thickened oil feedstock Properties
TABLE 2 operating conditions
| Item | Example 1 | Example 2 | Example 3 | Example 4 |
| Reaction temperature of | 400 | 420 | 450 | 410 |
| Pressure, MPa | 23 | 23 | 25 | 25 |
| Total reaction time, min | 4.9 | 5 | 2 | 2.6 |
| Weight ratio of deionized water to thickened oil raw material | 2:1 | 2:1 | 2:3 | 1:1 |
Table 3 data after thickened oil upgrading
| Item | Example 1 | Example 2 | Example 3 | Example 4 |
| Distribution of the product, weight% | ||||
| Pyrolysis gas | 2.0 | 2.3 | 3.7 | 2.7 |
| Light oil | 66.6 | 68.9 | 68.2 | 67.3 |
| Asphalt | 31.4 | 28.8 | 28.1 | 30.0 |
| Total up to | 100 | 100 | 100 | 100 |
TABLE 4 Pitch data
| Item | Example 1 | Example 2 | Example 3 | Example 4 |
| Softening point, DEG C | 126 | 135 | 140 | 129 |
| The four components are in percentage by weight | ||||
| Saturation fraction | 2.6 | 5.4 | 1.4 | 6.0 |
| Aromatic component | 24.8 | 20.6 | 22.2 | 21.3 |
| Glue | 31.2 | 28.8 | 30.1 | 29.4 |
| Asphaltenes | 41.4 | 45.2 | 46.3 | 43.3 |
It should be understood that the above-mentioned embodiments are only illustrative of the technical concepts and features of the present invention, and the purpose of the present invention is to enable people to understand the contents of the present invention and implement the present invention, and not to limit the protection scope of the present invention. All equivalent changes or modifications made according to the spirit of the main technical scheme of the invention are covered in the protection scope of the invention.
Claims (10)
1. A process for treating heavy oil with supercritical water and a supersonic separator, the process comprising the steps of:
1) respectively heating a deionized water flow and a thick oil to 50-90 ℃, pressurizing to 22.1-30 MPa, conveying to an inlet of a mixer, wherein the mass flow ratio of the thick oil to the deionized water flow is 0.2-4, mixing the thick oil and the deionized water in the mixer to obtain an oil-water mixed solution, heating the oil-water mixed solution to 400-500 ℃, and conveying to an inlet of a primary supercritical water reactor;
2) thick oil in the oil-water mixed solution is subjected to pyrolysis reaction in a first-stage supercritical water reactor and a second-stage supercritical water reactor in sequence, wherein the residence time of the thick oil in the first-stage supercritical water reactor is 1 s-5 min, the residence time of the thick oil in the second-stage supercritical water reactor is 5 s-10 min, and a mixed fluid of supercritical water, the modified thick oil and pyrolysis gas generated by the reaction is discharged from an upper outlet of the second-stage supercritical water reactor;
3) the mixed fluid in the step 2) enters from an inlet of the supersonic separator, the mixed fluid passes through a spray pipe in the supersonic separator, the axial speed and the tangential speed are increased, the temperature and the pressure are respectively lower than the critical temperature and the critical pressure of water, heavy components rich in asphaltene are separated out from a water-oil mutual solution system, continuously collide and coalesce into condensate, and are discharged from a liquid phase outlet under the action of centrifugation and air flow, the temperature of the liquid phase outlet is 330-370 ℃, the pressure of the liquid phase outlet is 12-16 MPa, the air flow is discharged from a gas phase outlet after the pressure of the air flow is restored through a diffuser, the pressure of the gas phase outlet is 14-18 MPa, and the temperature of the gas phase outlet is 350-390 ℃;
4) cooling the gas flow discharged from the gas phase outlet in the step 3) to 30-100 ℃, reducing the pressure to 0.1-0.5 MPa, transferring the gas flow into an oil-water separator, separating to obtain pyrolysis gas, light product oil and wastewater, conveying the condensate discharged from the liquid phase outlet in the step 3) into a granulation tower, and spraying the condensate through a nozzle and dispersing the condensate into solid particles rich in asphaltene.
2. The method for treating the thick oil together with the supercritical water and the supersonic separator according to claim 1, wherein the pressure of the deionized water and the thick oil after pressurization in the step 1) is 22.1-25 MPa.
3. The method for treating the thick oil together with the supercritical water and the supersonic speed separator according to claim 1, wherein the mass flow ratio of the thick oil and the deionized water stream in the step 1) is 1-2.
4. The method for treating the thick oil by using the supercritical water and the supersonic separator together according to claim 1, wherein the temperature of the oil-water mixed solution in the step 1) after being heated is 400-450 ℃.
5. The supercritical water and supersonic separator processing heavy oil together method according to claim 1, wherein the first stage supercritical water reactor and the second stage supercritical water reactor in step 2) are riser type upflow reactors, and the diameter of the second stage supercritical water reactor is 1.5-3 times of the diameter of the first stage supercritical water reactor.
6. The supercritical water and supersonic separator combined treatment method of thick oil according to claim 1, wherein the thick oil in step 2) stays in the first stage supercritical water reactor for 1-2 min, and the thick oil stays in the second stage supercritical water reactor for 1-4 min.
7. The method for treating thick oil by using supercritical water and a supersonic separator together according to claim 1, wherein the temperature of the cooled gas flow discharged from the gas phase outlet in the step 4) is 50-80 ℃.
8. The method for treating the thick oil by using the supercritical water and the supersonic speed separator together as claimed in claim 1, wherein the pressure of the depressurized gas flow discharged from the gas phase outlet in the step 4) is 0.1-0.2 MPa.
9. The supercritical water and supersonic separator combined thick oil treatment method according to claim 1, wherein the operating pressure of the prilling tower in step 4) is 5-20 MPa, and the operating temperature is controlled at 40-120 ℃.
10. The supercritical water and supersonic separator combined thick oil treatment method according to claim 1, wherein the operating pressure of the prilling tower in step 4) is 10-16 MPa, and the operating temperature is 50-100 ℃.
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| CN114790402A (en) * | 2022-02-28 | 2022-07-26 | 中海油天津化工研究设计院有限公司 | Method for continuously modifying oil product by supercritical water |
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