CN113801690A - Treatment method for extracting heavy oil by using supercritical water and solvent - Google Patents
Treatment method for extracting heavy oil by using supercritical water and solvent Download PDFInfo
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/14—Hydrocarbons
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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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
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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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
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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
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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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
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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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
- C10G2300/201—Impurities
- C10G2300/205—Metal content
- C10G2300/206—Asphaltenes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Abstract
The invention discloses a processing method for extracting heavy oil by using supercritical water and a solvent, which comprises the steps of heating and boosting heavy oil, water, the solvent and light distillate oil respectively, then mixing the raw materials and transmitting the mixture to a supercritical water reactor, carrying out cracking reaction on the heavy oil, cooling and depressurizing reaction products and then carrying out separation treatment, thereby realizing separation and solvent recovery of cracked gas, light distillate oil, medium distillate oil and deoiled asphalt products. The treatment method can effectively realize the lightening modification and separation of the heavy oil, the light distillate oil and the solvent play the role of a hydrogen donor in the modification process, the viscosity is obviously reduced, and the yield of the light oil is improved. The method has wide application range, and can also be used for treating substances such as petroleum, thickened oil, super-thickened oil, oil sand and the like.
Description
Technical Field
The invention relates to the technical field of petroleum treatment, in particular to a treatment method for extracting heavy oil by using supercritical water and a solvent.
Background
Heavy oil has high viscosity and is difficult to transport, and has impurities such as sulfur, nitrogen, metal elements, carbon residue, and the like, so that it is necessary to pretreat the heavy oil to upgrade the heavy oil.
Hydrotreating and solvent deasphalting are important processes for the pretreatment of heavy oils. The liquid phase oil obtained by hydrotreating has high yield and high quality, but the efficiency of the hydrotreating process is low because the hydrogen is difficult to dissolve in the oil product and the mass transfer resistance of the gas phase and the liquid phase is large. Solvent deasphalting is the separation of deasphalted oil and asphaltene components by utilizing the difference of the dissolving capacity of light hydrocarbon solvent to oil and asphaltene in heavy oil.
CN109790471A discloses a system and a method for solvent deasphalting, comprising a deasphalter and a controller device, the method for deasphalting by solvent extraction. However, the volume fraction of heavy oil and residue in the product separated by the method still exceeds 70%, and the partial product still has the problems of high viscosity, difficult transportation and the like. The deoiled asphalt has poor properties, and is mostly used for preparing road asphalt or used as a fuel and a raw material for delayed coking. The market selling price is low, and the utilization value is low.
The supercritical fluid technology can solve the problem of high content of heavy distillate oil in the solvent deasphalting process, reduce the viscosity and molecular mass of heavy oil and realize the purpose of heavy oil modification. The solubility of supercritical water is similar to that of an organic solvent, and the diffusivity is similar to that of gas, and heavy oil or asphalt can reduce the content of asphaltene in the heavy oil under the action of the supercritical water.
CN110114442A discloses a system and a method for deasphalting oil, which comprises pressurizing and heating oil and water, feeding the oil and water into a supercritical reactor for reaction to produce upgraded product, and realizing separation of light fraction, heavy fraction, gas and water by combining with reduced pressure separation process to produce deasphalted oil. However, the invention is that supercritical water directly treats heavy oil or asphalt components, and product separation is realized through a reduced pressure separation process, and certain bottleneck exists in the supercritical water treatment and separation capacity.
CN1307085A and CN1307086A disclose a method for thermal cracking of residue in a supercritical solvent and a method for catalytic cracking of residue in a supercritical solvent, respectively, which use multiple organic solvents to perform supercritical upgrading on heavy oil. Compared with an organic solvent, the supercritical water has the advantages of more thorough reaction, timely removal of reaction products out of an oil phase, avoidance of generation of coke and the like.
In order to solve the problems of the current heavy oil fraction treatment, it is necessary to develop a new heavy oil treatment method, which reduces the viscosity of the deoiled asphalt, improves the recovery rate of light oil, and simultaneously realizes continuous operation of the device, so as to increase the treatment capacity and realize industrial production.
Disclosure of Invention
The invention aims to provide a heavy oil treatment method for upgrading heavy oil with poor properties. The method applies the supercritical water and solvent co-extraction method to the treatment of the heavy oil, effectively realizes the modification of the heavy oil, obviously reduces the viscosity of the heavy oil, and improves the yield of the light oil product.
The technical scheme of the invention is as follows:
a treatment method for extracting heavy oil by using supercritical water and a solvent comprises the following steps:
a) heating a heavy oil raw material to 60-90 ℃, and conveying the heavy oil raw material, water, a solvent and light distillate oil to a mixer for mixing to obtain a mixed raw material, wherein the mass ratio of the water to the heavy oil raw material is 0.2: 1-5: 1, the mass ratio of the solvent to the heavy oil raw material is 0.1: 1-5: 1, and the mass ratio of the light distillate oil to the heavy oil raw material is 0.01: 1-0.25: 1;
b) the critical temperature of water is 374 ℃, the critical pressure is 22.1MPa, the state reached when the temperature and the pressure of the system exceed the critical point is called the supercritical state of the water, the mixed raw material obtained in the step a) is pressurized to 22.1-35 MPa, the mixed raw material is heated to 374-500 ℃, the water reaches the supercritical state, then the mixed raw material is fed into a supercritical water reactor, the mixed raw material stays in the supercritical water reactor for 30 seconds-40 minutes to generate pyrolysis reaction, a reaction product is obtained, light distillate oil and a solvent in the mixed raw material can be used as hydrogen supply agents for the reaction, the modification effect is improved, the lightening degree of a liquid phase product is improved, and the generation of a gas phase product is reduced;
c) cooling the reaction product obtained in the step b) to 237-266 ℃, reducing the pressure to 3-5 MPa, conveying the reaction product to a hot high-pressure separator, separating to obtain a gas-phase product and hot high-pressure oil, cooling the gas-phase product to 60-140 ℃, conveying the gas-phase product to a cold high-pressure separator, separating to obtain a pyrolysis gas product and an oil-water mixture, and conveying the oil-water mixture into an oil-water separator to separate to obtain wastewater and distillate oil;
d) pressurizing the hot high-molecular oil obtained in the step c) to 5-6 MPa, conveying the hot high-molecular oil to an asphalt separation tower, extracting a solvent from a solvent recovery tank, pressurizing the solvent to 5-6 MPa together with a fresh solvent, heating the solvent to 237-266 ℃, conveying the heated solvent to the asphalt separation tower, separating the solvent and the deasphalted oil through the asphalt separation tower, discharging a mixed solution of the solvent and the deasphalted oil from the tower top, and obtaining a deasphalted asphalt product from the tower bottom;
e) heating a mixed solution of the solvent and the deasphalted oil discharged from the top of the asphalt separation tower in the step d) to 267-330 ℃, then conveying the mixed solution to the deasphalted oil separation tower, obtaining the deasphalted oil at the bottom of the deasphalted oil separation tower, obtaining the solvent at the top of the tower, cooling, conveying the cooled solvent to a solvent recovery tank, extracting the solvent from the solvent recovery tank according to the mass ratio of the solvent to the heavy oil raw material in the step a), and conveying the extracted solvent to the mixer in the step a);
f) and (c) transferring the deasphalted oil obtained at the bottom of the deasphalted oil separation tower in the step e) and the distillate oil obtained by the oil-water separator in the step c) to a distillate oil separation tower, separating to obtain light distillate oil and medium distillate oil, transferring the light distillate oil to a light distillate oil recovery tank, and extracting the light distillate oil from the light distillate oil recovery tank according to the mass ratio of the light distillate oil to the heavy oil raw material in the step a) and transferring the light distillate oil to the mixer in the step a).
In the treatment method for extracting heavy oil by using supercritical water and a solvent, the selected solvent is heptane or a mixed solvent consisting of heptane and other light hydrocarbons, the other light hydrocarbons are one or more of propane, butane, pentane and hexane, and the mass ratio of the other light hydrocarbons to the heptane is 1: 2-1: 100.
In the above treatment method for supercritical water and solvent extraction of heavy oil, preferably, the mass ratio of water to heavy oil raw material in step a) is preferably 0.5:1 to 1:1, the mass ratio of solvent to heavy oil raw material is preferably 0.2:1 to 1.5:1, and the mass ratio of light distillate oil to heavy oil raw material is 0.01:1 to 0.1: 1.
In the above treatment method for extracting heavy oil with supercritical water and a solvent, the pressure of the pressurized mixed raw material in step b) is preferably 22.1 to 25Mpa, and the temperature after heating is preferably 374 to 430 ℃.
In the above supercritical water and solvent extraction heavy oil treatment method, preferably, the upflow supercritical water reactor in step b) is an upflow two-stage riser reactor, and the ratio of the inner diameter of the upper pipe to the inner diameter of the lower pipe is 1.5: 1-3: 1.
In the above supercritical water and solvent extraction heavy oil treatment method, preferably, the residence time of the mixed raw materials in the upflow supercritical water reactor in step b) is preferably 1 to 15 minutes.
In the above processing method for supercritical water and solvent extraction of heavy oil, preferably, the temperature of the reaction product in step c) after temperature reduction is preferably 240 to 255 ℃, and the pressure after pressure reduction is preferably 3.5 to 4 MPa.
In the above supercritical water and solvent heavy oil extraction treatment method, preferably, the temperature of the gas-phase reaction product in step d) after temperature reduction is preferably 60 to 80 ℃.
In the above treatment method for extracting heavy oil with supercritical water and a solvent, preferably, the mass ratio of the solvent in the asphalt separation tower in the step e) to the liquid phase product obtained by the hot high-pressure separator is preferably 2:1 to 3: 1.
In the treatment method for extracting heavy oil by supercritical water and solvent, the temperature of the mixed solution of the solvent and the deasphalted oil in the step f) is preferably 267-287 ℃.
The method organically combines supercritical water modification and solvent deasphalting processes, utilizes the solvent and the supercritical water to extract the heavy oil, can pyrolyze macromolecules such as colloid, asphaltene and the like in the heavy oil to generate micromolecules, realizes large-scale lightening transformation of the heavy oil, greatly reduces the viscosity, and can remove impurities such as carbon residue, sulfur, nitrogen, heavy metals and the like in the heavy oil. The subsequent solvent deasphalting process separates the heavy fraction oil into light fraction oil, medium fraction oil and deasphalted asphalt product. The treatment method can effectively realize the lightening modification and separation of the heavy oil, obviously reduce the viscosity and improve the yield of the light oil. The method has wide application range, and can also be used for treating substances such as petroleum, thickened oil, super-thickened oil, oil sand and the like.
Drawings
FIG. 1 is a schematic process flow diagram of a treatment process for extracting heavy oil using supercritical water and a solvent.
FIG. 2 is a schematic process flow diagram of a treatment process for extracting heavy oil using supercritical water and a solvent.
101 is a water preheater, 102 is a mixer, 103 is a booster pump, 104 is a heavy oil raw material preheater, 105-pass 106 is a heat exchanger, 107 is a heater, 108 is a supercritical water reactor, 109 is a back pressure valve, 110 is a hot high-pressure separator, 111 is a booster pump, 112 is an asphalt separating tower, 113 is a cooler, 114-pass 115 is a heater, 116 is a deasphalted oil separating tower, 117 is a solvent recovery tank, 118 is a fraction oil separating tower, 119 is a light distillate oil recovering tank, 120 is a cold high-pressure separator, 121 is an oil-water separator, 122-pass 123-pass 124 is a cooler, 201 is water, 202 is a heavy oil raw material, 203 is a fresh solvent, 204 is a solvent, 205 is a deasphalted asphalt product, 206 is a pyrolysis gas product, 207 is waste water, 208 is medium distillate oil, 209 is light distillate oil, and 210 is a light distillate oil product.
Detailed Description
The present invention will be further described in the following detailed description with reference to the drawings, but the invention is not limited thereto.
The invention provides a treatment method for extracting heavy oil by using supercritical water and a solvent, which comprises the following steps:
a) as shown in fig. 1, a heavy oil feedstock 202 is heated to 60-90 ℃ by a heavy oil feedstock preheater 104, and water 201, light distillate oil 209 and a solvent 204 are conveyed to a mixer 102 to be fully mixed, so as to obtain a mixed feedstock. Wherein the mass ratio of the water to the heavy oil raw material is 0.2: 1-5: 1, the mass ratio of the solvent to the heavy oil raw material is 0.1: 1-5: 1, and the mass ratio of the light distillate oil to the heavy oil raw material is 0.01: 1-0.25: 1.
b) Boosting the pressure of the mixed raw material obtained in the step a) to 22.1-35 MPa by using a booster pump 103, sequentially heating the mixed raw material by using a heat exchanger 105, a heat exchanger 106 and a heater 107 to 374-500 ℃, then introducing the mixed raw material through a lower inlet of a supercritical water reactor 108, and allowing the mixed raw material to stay in the supercritical water reactor 108 for 30 seconds-40 minutes to perform a pyrolysis reaction to obtain a reaction product.
c) And c) carrying out heat exchange on the reaction product obtained in the step b) and the mixed raw material through a heat exchanger 106, cooling to 237-266 ℃, reducing the pressure to 3-5 MPa through a back pressure valve 109, conveying to a hot high-pressure separator 110, separating to obtain a gas-phase product and hot high-fraction oil, carrying out heat exchange on the gas-phase product and the mixed raw material through a heat exchanger 105, cooling to 60-140 ℃ through a cooler 122, conveying to a cold high-pressure separator 120, separating through the cold high-pressure separator 120 to obtain a pyrolysis gas product stream 206 and an oil-water mixture, and conveying the oil-water mixture into an oil-water separator 121 to obtain wastewater 207 and distillate oil.
d) Boosting the pressure of the hot high-molecular oil obtained in the step c) to 5-6 MPa through a booster pump 111, conveying the hot high-molecular oil to an asphalt separation tower 112, extracting a solvent 204 from a solvent recovery tank 117, boosting the pressure to 5-6 MPa together with a fresh solvent 203, heating the hot high-molecular oil to 237-266 ℃ through a heater 114, conveying the hot high-molecular oil to the asphalt separation tower 112, obtaining a mixed solution of the solvent and deasphalted oil at the tower top of the asphalt separation tower 112, and obtaining a deoiled asphalt product 205 at the tower bottom.
e) Heating the mixed solution of the solvent and the deasphalted oil obtained at the top of the asphalt separating tower 112 in the step d) to 267-330 ℃ by a heater 115, then conveying the mixed solution to a deasphalted oil separating tower 116, obtaining the deasphalted oil at the bottom of the deasphalted oil separating tower 116, obtaining the solvent at the tower top, cooling the solvent, conveying the cooled solvent to a solvent recovery tank 117, extracting the solvent from the solvent recovery tank 117 according to the mass ratio of the solvent to the heavy oil raw material in the step a), and conveying the solvent to the mixer 102 in the step a).
f) And (e) the distillate oil obtained by the separation of the deasphalted oil separation tower 116 and the oil-water separator 121 in the step e) is conveyed to a distillate oil separation tower 118 to be separated into light distillate oil and medium distillate oil 208, the light distillate oil is conveyed to a light distillate oil recovery tank 119, the light distillate oil is extracted from the light distillate oil recovery tank according to the mass ratio of the light distillate oil to the heavy oil raw material in the step a) and conveyed to the mixer 102 in the step a), and the rest is extracted to be a light distillate oil product 210.
Another process for extracting heavy oil with supercritical water and solvent is provided in fig. 2, which comprises the following steps:
a) as shown in fig. 2, water 201 is heated to 60-90 ℃ by a water preheater 101, heavy oil raw material 202 is heated to 60-90 ℃ by a heavy oil raw material preheater 104, and light distillate oil 209 and solvent 204 are conveyed to a mixer 102 to be fully mixed, so as to obtain a mixed raw material. Wherein the mass ratio of the water to the heavy oil raw material is 0.2: 1-5: 1, the mass ratio of the solvent to the heavy oil raw material is 0.1: 1-5: 1, and the mass ratio of the light distillate oil to the heavy oil raw material is 0.01: 1-0.25: 1.
b) Boosting the pressure of the mixed raw material obtained in the step a) to 22.1-35 MPa by a booster pump 103, sequentially heating by a heater 107 to raise the temperature to 374-500 ℃, then introducing the mixed raw material through a lower inlet of a supercritical water reactor 108, and allowing the mixed raw material to stay in the supercritical water reactor 108 for 30 seconds-40 minutes to perform a pyrolysis reaction to obtain a reaction product.
c) Cooling the reaction product obtained in the step b) to 237-266 ℃ through a cooler 124, reducing the pressure to 3-5 MPa through a back pressure valve 109, conveying the reaction product to a hot high-pressure separator 110, separating to obtain a gas-phase product and hot high-pressure oil, cooling the gas-phase product to 60-140 ℃ through a cooler 122, conveying the gas-phase product to a cold high-pressure separator 120, separating through the cold high-pressure separator 120 to obtain a pyrolysis gas product stream 206 and an oil-water mixture, and allowing the oil-water mixture to enter an oil-water separator 121 to obtain wastewater 207 and distillate oil.
d) And c, boosting the pressure of the hot high-molecular oil obtained in the step c to 5-6 MPa through a booster pump 111, conveying the hot high-molecular oil to an asphalt separation tower 112, extracting a solvent 204 from a solvent recovery tank 117, boosting the pressure of the solvent 204 and a fresh solvent 203 to 5-6 MPa, heating the solvent and the fresh solvent to 237-266 ℃ through a heater 114, conveying the heated high-molecular oil to the asphalt separation tower 112, obtaining a mixed solution of the solvent and the deasphalted oil at the tower top of the asphalt separation tower 112, and obtaining a deoiled asphalt product 205 at the tower bottom.
e) Heating the mixed solution of the solvent and the deasphalted oil obtained at the top of the asphalt separating tower 112 in the step d) to 267-330 ℃ by a heater 115, then conveying the mixed solution to a deasphalted oil separating tower 116, obtaining the deasphalted oil at the bottom of the deasphalted oil separating tower 116, obtaining the solvent at the tower top, cooling the solvent, conveying the cooled solvent to a solvent recovery tank 117, extracting the solvent from the solvent recovery tank 117 according to the mass ratio of the solvent to the heavy oil raw material in the step a), and conveying the solvent to the mixer 102 in the step a).
f) And (e) the distillate oil obtained by the separation of the deasphalted oil separation tower 116 and the oil-water separator 121 in the step e) is conveyed to a distillate oil separation tower 118 to be separated into light distillate oil and medium distillate oil 208, the light distillate oil is conveyed to a light distillate oil recovery tank 119, the light distillate oil is extracted from the light distillate oil recovery tank according to the mass ratio of the light distillate oil to the heavy oil raw material in the step a) and conveyed to the mixer 102 in the step a), and the rest is extracted to be a light distillate oil product 210.
The present invention will be described in detail below by way of examples.
Example 1
a) After the heavy oil raw material is heated to 90 ℃, the heavy oil raw material, water, a solvent and light distillate oil are conveyed to a mixer to be mixed, so as to obtain a mixed raw material, wherein the mass ratio of the water to the heavy oil raw material is 0.2:1, the mass ratio of the solvent to the heavy oil raw material is 0.1:1, the mass ratio of the light distillate oil to the heavy oil raw material is 0.01:1, and the properties of the heavy oil product are shown in table 1.
b) Boosting the pressure of the mixed raw material obtained in the step a) to 22.1MPa, heating to 374 ℃, then, allowing the mixed raw material to enter through a lower inlet of a supercritical water reactor, allowing the mixed raw material to stay in the supercritical water reactor for 40 minutes, and performing pyrolysis reaction;
c) cooling the reaction product obtained in the step b) to 237 ℃, reducing the pressure to 3MPa, conveying the reaction product to a hot high-pressure separator, separating to obtain a gas-phase product and hot high-pressure oil, conveying the gas-phase product to a cold high-pressure separator after cooling, separating to obtain a pyrolysis gas product and an oil-water mixture, and conveying the oil-water mixture to an oil-water separator to separate to obtain wastewater and distillate oil;
d) boosting the pressure of the hot high-fraction oil obtained by separation of the hot high-pressure separator in the step c) to 6MPa, conveying the hot high-fraction oil to an asphalt separation tower, boosting and heating the solvent and the fresh solvent, conveying the solvent and the fresh solvent to the asphalt separation tower, separating the solvent and the fresh solvent by the asphalt separation tower, discharging a mixed solution of the solvent and the deasphalted oil from the tower top, and obtaining a deoiled asphalt product from the tower bottom;
e) heating the mixed solution of the solvent and the deasphalted oil obtained at the top of the asphalt separation tower in the step d) to 330 ℃, conveying the mixed solution to the deasphalted oil separation tower, obtaining the deasphalted oil at the bottom of the deasphalted oil separation tower, obtaining the solvent at the top of the tower, cooling, conveying the cooled solvent to a solvent recovery tank, extracting the solvent from the solvent recovery tank according to the mass ratio of the solvent to the heavy oil raw material of 0.1:1, and conveying the extracted solvent to a mixer;
f) and e) deasphalted oil obtained at the bottom of the deasphalted oil separation tower in the step e) and distillate oil obtained by separation of the oil-water separator in the step c) are conveyed to a distillate oil separation tower to be separated to obtain light distillate oil and medium distillate oil, the light distillate oil is conveyed to a light distillate oil recovery tank, and the light distillate oil is extracted from the light distillate oil recovery tank and conveyed to the mixer in the step a) according to the mass ratio of the light distillate oil to the heavy oil of 0.01: 1.
In the treatment method for extracting heavy oil by supercritical water and solvent, the selected solvent is heptane.
In the treatment method for extracting heavy oil by supercritical water and solvent, the supercritical water reactor in the step b) is an up-flow two-stage riser reactor, and the ratio of the inner diameter of an upper pipe to the inner diameter of a lower pipe is 1.5: 1.
The product analysis results are shown in Table 2. Wherein, the viscosity reduction rate refers to the difference between the viscosity of oil products in material flow after supercritical water treatment and the viscosity of heavy oil raw materials in a supercritical water reactor.
Example 2
a) After the heavy oil raw material is heated to 60 ℃, the heavy oil raw material, water, a solvent and light distillate oil are conveyed to a mixer to be mixed, so as to obtain a mixed raw material, wherein the mass ratio of the water to the heavy oil raw material is 5:1, the mass ratio of the solvent to the heavy oil raw material is 5:1, the mass ratio of the light distillate oil to the heavy oil raw material is 0.25:1, and the properties of the heavy oil product are shown in table 1.
b) Boosting the pressure of the mixed raw material obtained in the step a) to 35MPa, heating to 500 ℃, then, allowing the mixed raw material to enter through a lower inlet of a supercritical water reactor, allowing the mixed raw material to stay in the supercritical water reactor for 30 seconds, and performing pyrolysis reaction;
c) cooling the reaction product obtained in the step b) to 266 ℃, reducing the pressure to 5MPa, conveying the reaction product to a hot high-pressure separator, separating to obtain a gas-phase product and hot high-pressure oil, conveying the gas-phase product to a cold high-pressure separator after cooling, separating to obtain a pyrolysis gas product and an oil-water mixture, and conveying the oil-water mixture to an oil-water separator to separate to obtain wastewater and distillate oil;
d) boosting the pressure of the hot high-fraction oil obtained by separation of the hot high-pressure separator in the step c) to 5MPa, conveying the hot high-fraction oil to an asphalt separation tower, boosting and heating the solvent and the fresh solvent, conveying the solvent and the fresh solvent to the asphalt separation tower, separating the solvent and the fresh solvent by the asphalt separation tower, discharging a mixed solution of the solvent and the deasphalted oil from the tower top, and obtaining a deoiled asphalt product from the tower bottom;
e) heating the mixed solution of the solvent and the deasphalted oil obtained at the top of the asphalt separation tower in the step d) to 267 ℃, conveying the mixed solution to the deasphalted oil separation tower, obtaining the deasphalted oil at the bottom of the deasphalted oil separation tower, obtaining the solvent at the top of the tower, cooling, conveying the cooled solvent to a solvent recovery tank, extracting the solvent from the solvent recovery tank according to the mass ratio of the solvent to the heavy oil raw material of 5:1, and conveying the extracted solvent to a mixer;
f) and e) deasphalted oil obtained at the bottom of the deasphalted oil separation tower in the step e) and distillate oil obtained by separation of the oil-water separator in the step c) are conveyed to a distillate oil separation tower to be separated to obtain light distillate oil and medium distillate oil, the light distillate oil is conveyed to a light distillate oil recovery tank, and the light distillate oil is extracted from the light distillate oil recovery tank and conveyed to the mixer in the step a) according to the mass ratio of the light distillate oil to the heavy oil of 0.25: 1.
In the treatment method for extracting the heavy oil by using the supercritical water and the solvent, the selected solvent is a mixed solvent of heptane and hexane, and the mass ratio of the heptane to the hexane is 100: 1.
In the above supercritical water and solvent extraction heavy oil treatment method, the upflow supercritical water reactor in step b) is an upflow two-stage riser reactor, and the ratio of the inner diameter of the upper pipe to the inner diameter of the lower pipe is 1.5: 1.
The product analysis results are shown in Table 2. Wherein, the viscosity reduction rate refers to the difference between the viscosity of oil products in material flow after supercritical water treatment and the viscosity of heavy oil raw materials in a supercritical water reactor.
Example 3
a) The heavy oil raw material is oil sand asphalt, the oil sand asphalt is heated to 90 ℃, water is heated to 90 ℃, then the heavy oil raw material, the water, the solvent and the light distillate oil are conveyed to a mixer to be mixed to obtain a mixed raw material, the mass ratio of the water to the heavy oil raw material is 1:1, the mass ratio of the solvent to the heavy oil raw material is 0.4:1, the mass ratio of the light distillate oil to the heavy oil raw material is 0.25:1, and the properties of the heavy oil product are shown in table 1.
b) Boosting the pressure of the mixed raw material obtained in the step a) to 25MPa, heating to 420 ℃, then, introducing the mixed raw material through a lower inlet of a supercritical water reactor, wherein the mixed raw material stays in the supercritical water reactor for 10 minutes, and carrying out pyrolysis reaction;
c) cooling the reaction product obtained in the step b) to 260 ℃, reducing the pressure to 4MPa, conveying the reaction product to a hot high-pressure separator, separating to obtain a gas-phase product and hot high-pressure oil, conveying the gas-phase product to a cold high-pressure separator after cooling, separating to obtain a pyrolysis gas product and an oil-water mixture, and allowing the oil-water mixture to enter an oil-water separator to separate to obtain wastewater and distillate oil;
d) boosting the pressure of the hot high-fraction oil obtained by separation of the hot high-pressure separator in the step c) to 5.5MPa, conveying the hot high-fraction oil to an asphalt separation tower, boosting and heating the solvent and the fresh solvent, conveying the solvent and the fresh solvent to the asphalt separation tower, separating the solvent and the fresh solvent by the asphalt separation tower, discharging a mixed solution of the solvent and deasphalted oil from the tower top, and obtaining a deoiled asphalt product from the tower bottom;
e) heating the mixed solution of the solvent and the deasphalted oil obtained at the top of the asphalt separating tower in the step d) to 290 ℃, conveying the mixed solution to the deasphalted oil separating tower, obtaining the deasphalted oil at the bottom of the deasphalted oil separating tower, obtaining the solvent at the top of the tower, cooling, conveying the cooled solvent to a solvent recovery tank, extracting the solvent from the solvent recovery tank according to the mass ratio of the solvent to the heavy oil raw material of 0.4:1, and conveying the extracted solvent to a mixer;
f) and e) deasphalted oil obtained at the bottom of the deasphalted oil separation tower in the step e) and distillate oil obtained by separation of the oil-water separator in the step c) are conveyed to a distillate oil separation tower to be separated to obtain light distillate oil and medium distillate oil, the light distillate oil is conveyed to a light distillate oil recovery tank, and the light distillate oil is extracted from the light distillate oil recovery tank and conveyed to the mixer in the step a) according to the mass ratio of the light distillate oil to the heavy oil of 0.25: 1.
In the treatment method for extracting the heavy oil by using the supercritical water and the solvent, the selected solvent is a mixed solvent of heptane and pentane, and the mass ratio of the heptane to the hexane is 2: 1.
In the above supercritical water and solvent extraction heavy oil treatment method, the upflow supercritical water reactor in step b) is an upflow two-stage riser reactor, and the ratio of the inner diameter of the upper pipe to the inner diameter of the lower pipe is 3: 1.
The product analysis results are shown in Table 2. Wherein, the viscosity reduction rate refers to the difference between the viscosity of oil products in material flow after supercritical water treatment and the viscosity of heavy oil raw materials in a supercritical water reactor.
TABLE 1 oil feedstock Properties
Table 2 oil quality modification data
| Item | Example 1 | Example 2 | Example 3 |
| Viscosity reduction rate% | 91.2 | 99.3 | 97.0 |
| Distribution of the product, weight% | |||
| Pyrolysis gas | 1.1 | 3.7 | 2.1 |
| Light distillate oil | 17.8 | 24.5 | 19.5 |
| Middle distillate | 21.2 | 20.5 | 22.2 |
| Heavy oil | 59.9 | 51.3 | 56.2 |
| Total up to | 100 | 100 | 100 |
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 treatment method for extracting heavy oil by using supercritical water and a solvent comprises the following steps:
a) heating a heavy oil raw material to 60-90 ℃, and conveying the heavy oil raw material, water, a solvent and light distillate oil to a mixer for mixing to obtain a mixed raw material, wherein the mass ratio of the water to the heavy oil raw material is 0.2: 1-5: 1, the mass ratio of the solvent to the heavy oil raw material is 0.1: 1-5: 1, and the mass ratio of the light distillate oil to the heavy oil raw material is 0.01: 1-0.25: 1;
b) boosting the pressure of the mixed raw material obtained in the step a) to 22.1-35 MPa, heating to 374-500 ℃ to enable water to reach a supercritical state, introducing the mixed raw material into a supercritical water reactor, and allowing the mixed raw material to stay in the supercritical water reactor for 0.5-40 minutes to perform a pyrolysis reaction to obtain a reaction product;
c) cooling the reaction product obtained in the step b) to 237-266 ℃, reducing the pressure to 3-5 MPa, conveying the reaction product to a hot high-pressure separator, separating to obtain a gas-phase product and hot high-pressure oil, cooling the gas-phase product to 60-140 ℃, conveying the gas-phase product to a cold high-pressure separator, separating to obtain a pyrolysis gas product and an oil-water mixture, and conveying the oil-water mixture into an oil-water separator to separate to obtain wastewater and distillate oil;
d) pressurizing the hot high-molecular oil obtained in the step c) to 5-6 MPa, conveying the hot high-molecular oil to an asphalt separation tower, extracting a solvent from a solvent recovery tank, pressurizing the solvent to 5-6 MPa together with a fresh solvent, heating the solvent to 237-266 ℃, conveying the heated solvent to the asphalt separation tower, separating the solvent and the deasphalted oil through the asphalt separation tower, discharging a mixed solution of the solvent and the deasphalted oil from the tower top, and obtaining a deasphalted asphalt product from the tower bottom;
e) heating a mixed solution of the solvent and the deasphalted oil discharged from the top of the asphalt separation tower in the step d) to 267-330 ℃, then conveying the mixed solution to the deasphalted oil separation tower, obtaining the deasphalted oil at the bottom of the deasphalted oil separation tower, obtaining the solvent at the top of the tower, cooling, conveying the cooled solvent to a solvent recovery tank, extracting the solvent from the solvent recovery tank according to the mass ratio of the solvent to the heavy oil raw material in the step a), and conveying the extracted solvent to the mixer in the step a);
f) and (c) transferring the deasphalted oil obtained at the bottom of the deasphalted oil separation tower in the step e) and the distillate oil obtained by the oil-water separator in the step c) to a distillate oil separation tower, separating to obtain light distillate oil and medium distillate oil, transferring the light distillate oil to a light distillate oil recovery tank, and extracting the light distillate oil from the light distillate oil recovery tank according to the mass ratio of the light distillate oil to the heavy oil raw material in the step a) and transferring the light distillate oil to the mixer in the step a).
2. The process of claim 1, wherein the solvent is heptane or a mixture of heptane and other light hydrocarbons.
3. The treatment method for extracting heavy oil by using supercritical water and a solvent as claimed in claim 2, wherein the other light hydrocarbon is one or more of propane, butane, pentane and hexane, and the mass ratio of the other light hydrocarbon to heptane is 1: 2-1: 100.
4. The treatment method for extracting heavy oil by using supercritical water and a solvent, according to claim 1, wherein the mass ratio of the water to the heavy oil raw material in the step a) is 0.5:1 to 1:1, the mass ratio of the solvent to the heavy oil raw material is 0.2:1 to 1.5:1, and the mass ratio of the light distillate oil to the heavy oil raw material is 0.01:1 to 0.1: 1.
5. The processing method for extracting heavy oil by using supercritical water and a solvent as claimed in claim 1, wherein the pressure of the pressurized mixed raw material in step b) is 22.1-25 Mpa, and the temperature after heating is 374-430 ℃.
6. The treatment method for extracting heavy oil by using supercritical water and a solvent as claimed in claim 1, wherein the supercritical water reactor in step b) is an up-flow two-stage riser reactor, and the ratio of the inner diameter of the upper pipe to the inner diameter of the lower pipe is 1.5: 1-3: 1.
7. The process of claim 1, wherein the residence time of the mixed raw material in step b) in the supercritical water reactor is 1-15 min.
8. The treatment method for extracting heavy oil by using supercritical water and a solvent as claimed in claim 1, wherein the temperature of the reaction product in step c) after being cooled is 240-255 ℃, and the pressure after being reduced is 3.5-4 MPa.
9. The treatment method for extracting heavy oil by using supercritical water and a solvent as claimed in claim 1, wherein the temperature of the gas phase reaction product in the step d) after being cooled is 60-80 ℃.
10. The treatment method for extracting heavy oil by using supercritical water and a solvent as claimed in claim 1, wherein the mass ratio of the solvent to the hot high-purity oil in the asphalt separation tower in the step e) is 2: 1-3: 1, and the preferable heating temperature is 267-287 ℃.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114790401A (en) * | 2022-02-28 | 2022-07-26 | 中国海洋石油集团有限公司 | Combined method for heavy oil modification |
| 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 |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101077980A (en) * | 2006-05-26 | 2007-11-28 | 华东理工大学 | Method for preparing light oil from supercritical water modified vacuum residuum |
| CN101942337A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Combined process for heavy oil modification |
| CN110114442A (en) * | 2017-01-04 | 2019-08-09 | 沙特阿拉伯石油公司 | For the deasphalting system and method for oil |
-
2021
- 2021-09-10 CN CN202111063192.7A patent/CN113801690B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101077980A (en) * | 2006-05-26 | 2007-11-28 | 华东理工大学 | Method for preparing light oil from supercritical water modified vacuum residuum |
| CN101942337A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Combined process for heavy oil modification |
| CN110114442A (en) * | 2017-01-04 | 2019-08-09 | 沙特阿拉伯石油公司 | For the deasphalting system and method for oil |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114790401A (en) * | 2022-02-28 | 2022-07-26 | 中国海洋石油集团有限公司 | Combined method for heavy oil modification |
| 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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