CN115449396A - Visbreaking device and visbreaking method - Google Patents
Visbreaking device and visbreaking method Download PDFInfo
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- CN115449396A CN115449396A CN202110639024.1A CN202110639024A CN115449396A CN 115449396 A CN115449396 A CN 115449396A CN 202110639024 A CN202110639024 A CN 202110639024A CN 115449396 A CN115449396 A CN 115449396A
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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
- 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
Abstract
The invention provides a visbreaking device and a visbreaking method. The visbreaking device comprises a raw material supply unit, a viscosity reducing unit and a viscosity reducing unit, wherein the raw material supply unit comprises a raw material oil supply device and a water supply device; the heating unit is provided with a raw material inlet and a hot mixture outlet, and the raw material inlet is connected with the raw oil supply device and the water supply device; the gas-liquid separation unit is provided with an inlet of the object to be separated, an outlet of the gaseous object to be separated and an outlet of the liquid object to be separated, the inlet of the object to be separated is connected with the outlet of the hot mixture, the gas-liquid separation unit is used for carrying out gas-liquid separation on the hot mixture to obtain the gaseous object to be separated and the liquid object to be separated, and the gaseous object to be separated comprises water and light gas oil; and the visbreaking unit is connected with the liquid isolate outlet and is used for leading the liquid isolate to carry out visbreaking reaction. The gas-liquid separation unit is used for separating water and light gas oil components before the visbreaking unit, so that the problems of condensation coking, influence on product stability and the like caused by overlong reaction time of partial materials due to material back mixing are avoided.
Description
Technical Field
The invention relates to the technical field of petroleum processing, in particular to a visbreaking device and a visbreaking method.
Background
With the increasing world economy and the increasing demand of petroleum, the conventional petroleum resources cannot meet the demand of people, and the heavy crude oil becomes the main raw material in the current petroleum processing. The visbreaking has the characteristics of mature technology, less investment, easy construction, low operation cost, low requirement on raw materials and the like, and plays an important role in the heavy oil processing technology.
The visbreaking process is one of the effective ways to lighten heavy inferior oil. Visbreaking is a parallel sequential reaction process in which both cracking and condensation reactions occur. In actual production, it is desired to increase the cracking reaction depth of the visbreaking process to obtain high visbreaking efficiency, but increasing the cracking reaction depth requires increasing the reaction temperature or increasing the reaction time, which increases the condensation reaction, causes coking, causes problems such as equipment blockage, and shortens the production cycle. In contrast, shallow visbreaking reactions do not achieve high visbreaking efficiency. In addition, the viscosity-reducing oil stability is reduced with the enhancement of the condensation reaction, so that the fuel oil is layered until precipitation, and the product storage and transportation are influenced. Therefore, the difficult problem to be solved is how to balance the relationship between the normal operation of the device and the improvement of the visbreaking reaction depth.
The key problem of visbreaking is how to make the visbreaking reaction uniform, keep the materials in the reaction unit in a horizontal thrust state and reduce back mixing. The material backmixing in the visbreaking reaction tower widens the material retention time, the material with too short retention time can not reach the expected conversion depth, and the material with too long retention time can generate over-cracking, so that the condensation side reaction is increased, coking is caused, and the stability of the product is adversely affected. Therefore, in order to ensure the stability of the product and the long-period operation of the device, the device can only be operated at a proper cracking depth to ensure that the material with overlong retention time can not be coked and the stability of the product can not be influenced, so that the backmixing degree of the material in the visbreaking reaction unit is the most critical factor for limiting and improving the visbreaking reaction depth, namely, for the same raw material, the backmixing degree of the material in the visbreaking reaction unit is smaller, and on the premise of ensuring the long-period stable operation of the device and the stability of the product, the visbreaking reaction depth can be deeper, namely, the visbreaking efficiency is higher.
At present, in order to reduce the back mixing of materials in the visbreaking reaction unit, a transverse sieve plate is generally arranged in the visbreaking tower to reduce the back mixing, however, practice proves that the method has limited effect, the back mixing of materials in the visbreaking reaction unit cannot be effectively controlled in the prior art, and the visbreaking reaction depth is difficult to be increased, namely the visbreaking efficiency is further improved.
Disclosure of Invention
The invention mainly aims to provide a visbreaking device and a visbreaking method, which aim to solve the problem that the backmixing of materials in a visbreaking reaction unit cannot be effectively controlled in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided a visbreaking apparatus comprising: a raw material supply unit including a raw material oil supply device and a water supply device; the heating unit is provided with a raw material inlet and a hot mixture outlet, and the raw material inlet is connected with the raw oil supply device and the water supply device; the gas-liquid separation unit is provided with an inlet of a to-be-separated object, an outlet of a gaseous separated object and an outlet of a liquid separated object, the inlet of the to-be-separated object is connected with the outlet of the hot mixture, the gas-liquid separation unit is used for carrying out gas-liquid separation on the hot mixture to obtain the gaseous separated object and the liquid separated object, and the gaseous separated object comprises water and light gas oil; and the viscosity breaking unit is connected with the liquid separated matter outlet and is used for enabling the liquid separated matter to carry out viscosity breaking reaction.
Furthermore, in the visbreaking device, the visbreaking unit comprises a visbreaking reaction tower, the visbreaking reaction tower is provided with an inlet for the material to be cracked and an outlet for the produced oil from visbreaking, the inlet for the material to be cracked is connected with the outlet for the liquid isolate, the inlet for the material to be cracked is arranged at the bottom of the visbreaking reaction tower, and the outlet for the produced oil from visbreaking is arranged at the top of the visbreaking reaction tower.
Further, in the above visbreaking apparatus, the visbreaking apparatus further comprises: and the fractionating equipment (6) is connected with the viscosity breaking produced oil outlet and is used for fractionating the viscosity breaking produced oil.
According to another aspect of the present invention, there is provided a visbreaking process comprising: step S1: heating a mixture comprising raw oil and water to obtain a hot mixture; step S2: carrying out gas-liquid separation on the hot mixture to obtain a gaseous separated matter and a liquid separated matter, wherein the gaseous separated matter comprises water and light gas oil; and step S3: and performing visbreaking on the liquid isolate to obtain the visbroken product oil.
Further, in the above visbreaking process, the visbreaking process further comprises: and S4, fractionating the visbreaking oil to obtain cracked gas, cracked gasoline and visbreaking residual oil.
Further, in the above visbreaking method, in step S1, the mass ratio of water to feed oil is 0.3 to 1.8.
Further, in the above visbreaking method, in step S1, the temperature of the hot mixture is 370 to 460 ℃.
Further, in the above visbreaking method, the visbreaking is performed at a pressure of 0.2 to 0.7 MPa.
Further, in the above visbreaking method, the step S3 includes performing a visbreaking reaction on the liquid isolate for 20 minutes to 200 minutes.
Further, in the above visbreaking method, the gaseous separated material obtained in step S2 is fractionated together with the visbroken product oil in step S3.
Further, in the above visbreaking method, the feedstock oil includes super heavy crude oil, atmospheric residue, vacuum residue, or deoiled asphalt.
The visbreaking device and the visbreaking method overcome the problems in the prior art, and achieve the technical effects of enabling the visbreaking reaction to be more uniform, enabling the visbreaking temperature to be higher and the reaction time to be longer, and enabling the visbreaking reaction depth to be increased.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 shows a schematic diagram of a visbreaker according to the invention.
Detailed Description
It should be noted that, in the present application, the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail with reference to examples.
It can be understood from the foregoing background art that the visbreaking method in the prior art cannot effectively solve the problem of back-mixing of the materials in the visbreaking reaction unit, thereby affecting the further improvement of the visbreaking reaction depth. In response to the technical problems described above, the present application provides a visbreaker and a visbreaking method.
In an exemplary embodiment of the present application, there is provided a visbreaker, as shown in fig. 1, including a feedstock supply unit including a feedstock oil supply device 1 and a water supply device 2, a heating unit 3, a gas-liquid separation unit 4, and a visbreaker unit 5; the heating unit 3 is provided with a raw material inlet and a hot mixture outlet, and the raw material inlet is connected with the raw oil supply device 1 and the water supply device 2; the gas-liquid separation unit 4 is provided with a to-be-separated object inlet, a gaseous separated object outlet and a liquid separated object outlet, the to-be-separated object inlet is connected with the hot mixture outlet, the gas-liquid separation unit 4 is used for carrying out gas-liquid separation on the hot mixture to obtain a gaseous separated object and a liquid separated object, and the gaseous separated object comprises water and light gas oil; and the visbreaking unit 5 is connected to the liquid separator outlet for subjecting the liquid separator to a visbreaking reaction.
In the above embodiment, the stock oil and water in the stock oil supply device 1 and the water supply device 2 are pumped into the heating unit 3 via the stock material inlet. In the heating unit 3 the feed oil is mixed with water and heated to a hot mixture. The hot mixture is conveyed to the gas-liquid separation unit 4 through the hot mixture outlet of the heating unit 3 and the inlet of the substance to be separated. In the gas-liquid separation unit 4, the hot mixture is separated into a gaseous separated matter and a liquid separated matter by the gas-liquid separation tank, wherein the gaseous separated matter includes water vapor and light gas oil. The water vapor and the light gas oil are discharged through a gas-liquid separation outlet of the gas-liquid separation unit 4, and the liquid-state separation is discharged through a liquid-state separation outlet of the gas-liquid separation unit 4 and conveyed to the visbreaking unit 5. In the visbreaking unit 5, the liquid isolate is subjected to a visbreaking reaction to produce a visbroken product oil of reduced viscosity.
Unlike prior art visbreakers, water and light gas oil components have been removed from the feed oil prior to visbreaking by use of the visbreaker of the present application. In the subsequent visbreaking reaction, as the reaction system does not contain water and light gas oil components, deeper visbreaking reaction can be carried out, the material back mixing caused by the water and the light gas oil components is avoided, the material is carried out in a reaction tower in a nearly plug flow state, and the problems of condensation coking, product stability influence and the like caused by overlong reaction time of partial material due to the material back mixing are further avoided. In addition, the problem of material back-mixing caused by gas-phase components such as water and light gas oil is solved, so that the reaction temperature can be increased or the reaction time can be prolonged, the visbreaking raw oil is fully visbroken, the viscosity of the raw material is reduced, the visbroken residual oil with lower viscosity is produced, and more light distillate oil is produced.
In some embodiments of the present application, as shown in fig. 1, it is preferable that the visbreaking unit 5 includes a visbreaking reaction tower having an inlet for a material to be cracked and an outlet for a visbroken product oil, the inlet for the material to be cracked is connected to the outlet for the liquid separated material, the inlet for the material to be cracked is disposed at the bottom of the visbreaking reaction tower, and the outlet for the visbroken product oil is disposed at the top of the visbreaking reaction tower. In the present embodiment, the liquid separator outlet of the gas-liquid separation unit 4 is connected to the inlet of the material to be cracked, which is provided at the bottom of the visbreaking reaction tower, so that the liquid separator obtained through the gas-liquid separation is conveyed into the visbreaking reaction tower. After the liquid separated matter undergoes visbreaking reaction, the produced visbreaking product oil is discharged through a visbreaking product oil outlet arranged at the top of the visbreaking reaction tower.
In one embodiment of the present application, as shown in fig. 1, it is preferred that the visbreaking apparatus further comprises a fractionation device 6. The fractionating device 6 is connected with the viscosity breaking produced oil outlet and is used for fractionating the viscosity breaking produced oil. After the liquid isolate undergoes visbreaking reaction, the visbreaking product oil produced contains light distillate oil. And introducing the visbreaking produced oil into a fractionating device 6 through a visbreaking produced oil outlet to obtain cracked gas, cracked gasoline and visbreaking residual oil. The visbroken resid can be used as a fuel oil or a blending component for fuel oil. The gas phase separated in the gas-liquid separation tank may be used and the light gas oil obtained through condensation may be used as the intermediate product. In a preferred embodiment, the gas phase separation or light gas oil may be mixed with visbreaking product oil and then fractionated.
In another exemplary embodiment of the present application, there is provided a visbreaking process comprising: step S1: heating a mixture comprising raw oil and water to obtain a hot mixture; step S2: carrying out gas-liquid separation on the hot mixture to obtain a gaseous separated matter and a liquid separated matter, wherein the gaseous separated matter comprises water and light gas oil; and step S3: and carrying out viscosity breaking reaction on the liquid isolate to obtain viscosity breaking produced oil.
Unlike the prior art visbreaking process, in the process of the present application, the feedstock oil is first mixed with water and the resulting mixture is heated, resulting in a hot mixture. And carrying out gas-liquid separation on the obtained hot mixture so as to separate the hot mixture into a gaseous separated matter and a liquid separated matter, wherein the gaseous separated matter comprises water and light gas oil, and then carrying out viscosity breaking reaction on the separated liquid separated matter. Since the visbreaking process of the present application employs a step of gas-liquid separating a hot mixture comprising feedstock oil and water, water and light gas oil components that affect the back-mixing of the feedstock oil have been removed from the feedstock oil prior to visbreaking. In the subsequent visbreaking reaction, as the reaction system does not contain water and light gas oil components any more, the visbreaking reaction is more uniform, and the problem of coking caused by transition condensation of partial materials due to back mixing caused by the water-containing light gas oil components is avoided. In addition, because the visbreaking reaction is uniform, more severe reaction conditions can be adopted in the visbreaking reaction, so that the components of the liquid isolate (including the heavy raw oil) in the reaction can be fully visbroken, thereby improving the yield of the product light distillate and the efficiency of visbreaking.
In some embodiments of the present application, the visbreaking process further comprises a step S4 of fractionating the visbroken product oil to obtain cracked gas, cracked gasoline, and visbroken bottoms. After visbreaking to obtain the visbroken product oil, the visbroken product oil may be fractionated to obtain cracked gas, cracked gasoline, and visbroken residue. The visbroken resid can be used as a fuel oil or a blending component for fuel oil. The gas phase separator obtained by separating the gas-liquid separation tank can be condensed to obtain light gas oil which is directly used as an intermediate product; or mixing the gas phase separated matter with viscosity breaking oil and fractionating.
In some embodiments of the present application, in step S1, the mass ratio of water to feedstock oil is preferably 0.3. Since direct heating of the feedstock will cause coking of the feedstock in the furnace tubes, in some embodiments of the present application, it is necessary to mix the feedstock with water prior to heating. In a preferred embodiment, the mass ratio of water to feedstock oil is 0.3 to 1.8. Within the range, the raw oil can be effectively prevented from coking at the tube wall position of the furnace tube of the heating furnace in the heating process.
In some embodiments of the present application, it is preferred that in step S1, the temperature of the hot mixture is in the range of 370 ℃ to 460 ℃. In some embodiments of the present application, since water has been added in step S1, the mixture of the feedstock oil and water may be heated to 370 ℃ to 460 ℃. In the temperature range, the retention time of the raw oil in the furnace tube is shortened due to the vaporization of water, so that the raw oil cannot coke on the furnace wall of the heating furnace, and the gas-liquid separation can be quickly realized in the subsequent gas-liquid separation process.
In some embodiments herein, it is preferred that the above-described visbreaking reaction is carried out at a pressure of from 0.2MPa to 0.7 MPa. In some embodiments of the present application, deeper visbreaking reactions can be performed under more severe conditions due to the visbreaking process of the present application.
In some embodiments of the present application, the step S3 further comprises performing a viscosity breaking reaction on the liquid isolate for 20 minutes to 200 minutes. In some embodiments herein, in the visbreaking reaction of step S3, the reaction may be conducted under more severe conditions. Preferably, the visbreaking reaction is carried out on the liquid isolate obtained by gas-liquid separation for 20 minutes to 200 minutes at the outlet temperature of the heating furnace of 370 ℃ to 460 ℃. In the temperature and time range, the visbreaking reaction of the raw oil can be fully generated, and the yield of the light distillate oil can be improved.
In some embodiments of the present application, the visbreaking process further comprises fractionating the gaseous isolate separated in step S2 together with the visbroken product oil in step S3.
In some embodiments of the present application, the feedstock oil comprises ultra-thick feedstock oil or resid. In the present application, the raw oil that can be used includes ultra-thick crude oil, atmospheric residue, vacuum residue, deoiled asphalt, and the like.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the present application as claimed.
In the present application, the toluene insoluble (coke) content (mass fraction) of the visbreaking product oil or the oil mixed with light gas oil was determined by the method of GB 2292-2018. The reaction behavior was investigated with the viscosity-reducing conversion, defined as follows: viscosity breaking conversion rate = (cracked gas mass + cracked gasoline mass)/raw oil mass. The viscosity-reducing residual oil stability adopts ASTM D4740-04 (2014) spot test method, the test result is totally 5 grades, the lower the grade number is, the better the relative stability is, generally, the result is below grade 3, namely, grade 2, grade 1 stability can meet the oil stability requirement.
Examples
Example 1
The Liaohe super heavy oil is used as raw oil, wherein the density of the raw oil at 20 ℃ is 1004.6kg/m 3 And a kinematic viscosity at 100 ℃ of 905.6mm 2 The carbon residue was 13.72wt%, and the content of fractions less than 165 ℃ and the content of residual oil more than 350 ℃ in the feed oil were 0.01wt% and 91.1wt%.
The experiment is carried out in a pilot scale viscosity breaking device, raw oil and water are mixed, the mass ratio of the water to the raw oil is 0.5wt%, the mixture enters a heating unit, namely a heating furnace, for heating, the temperature at the outlet of the furnace is 435 ℃, the heated material enters a gas-liquid separation unit, namely a gas-liquid separation tank, for gas-liquid separation, the water and the light gas oil flow out from the outlet at the top of the gas-liquid separation tank, light gas oil is obtained by condensation, the liquid phase part flows out from the outlet at the bottom of the gas-liquid separation tank, enters the viscosity breaking tower from the bottom of the viscosity breaking tower for viscosity breaking, the viscosity breaking generated oil flows out from the top of the viscosity breaking tower, the pressure at the top of the viscosity breaking tower is 0.7MPa, the liquid phase part stays in the viscosity breaking tower for 50 minutes, the viscosity breaking generated oil and the light gas oil are mixed and enter a fractionating tower for fractionating, cracked gas and cracked gasoline are obtained at the top of the tower, and viscosity breaking residual oil is obtained at the bottom of the tower.
The toluene insoluble (coke) content of the viscosity-reduced oil and light gas oil mixed oil is 0.17% (mass fraction), the viscosity-reduction conversion rate is 5.4%, and the kinematic viscosity of the viscosity-reduced residual oil at 100 ℃ is 125.2mm 2 And s. The speckle test result of the viscosity-reduced residual oil is grade 2, and the viscosity-reduced residual oil has good stability.
Comparative example 1
Liaohe super heavy oil is used as raw oil, wherein the density of the raw oil at 20 ℃ is 1004.6kg/m 3 And a kinematic viscosity at 100 ℃ of 905.6mm 2 The carbon residue was 13.72wt%, and the content of fractions less than 165 ℃ in the feed oil was 0.01wt% and the content of residues more than 350 ℃ was 91.1wt%.
The experiment is carried out in a pilot-scale viscosity breaking device, raw oil is mixed with water, the mass ratio of the water to the raw oil is 0.5wt%, the mixture enters a heating unit, namely a heating furnace, to be heated, the temperature of a furnace outlet is 435 ℃, the heated material enters the viscosity breaking tower from the bottom of the viscosity breaking tower to be subjected to viscosity breaking, the viscosity breaking generated oil flows out of the top of the viscosity breaking tower, the pressure of the top of the viscosity breaking tower is 0.7MPa, the retention time of the material in the viscosity breaking tower is 50 minutes, the viscosity breaking generated oil enters a fractionating tower to be fractionated, cracked gas and cracked gasoline are obtained at the top of the tower, and viscosity breaking residual oil is obtained at the bottom of the tower.
The viscosity-reduced oil had a toluene-insoluble (coke) content of 0.58% (mass fraction), a viscosity-reduction conversion of 4.8%, and a kinematic viscosity of the viscosity-reduced residue at 100 ℃ of 181.8mm 2 And/s, the speckle test result of the viscosity-reduced residual oil is grade 3, and the stability of the viscosity-reduced residual oil does not meet the requirement of less than grade 3.
Example 2
Liaohe super heavy oil is used as raw oil, wherein the density of the raw oil at 20 ℃ is 1004.6kg/m 3 A kinematic viscosity at 100 ℃ of 905.6mm 2 The carbon residue was 13.72wt%, and the content of fractions less than 165 ℃ and the content of residual oil more than 350 ℃ in the feed oil were 0.01wt% and 91.1wt%.
The experiment is carried out in a pilot-scale viscosity breaking device, raw oil and water are mixed, the mass ratio of the water to the raw oil is 0.3wt%, the mixture enters a heating unit, namely a heating furnace, to be heated, the temperature of a furnace outlet is 370 ℃, the heated material enters a gas-liquid separation tank, after gas-liquid separation, the water and light gas oil are discharged from the top outlet of the gas-liquid separation unit, a liquid phase part flows out from the bottom outlet of the gas-liquid separation tank, enters the viscosity breaking tower from the bottom of the viscosity breaking tower to be subjected to viscosity breaking, viscosity breaking generated oil flows out from the top of the viscosity breaking tower, the pressure at the top of the viscosity breaking tower is 0.2MPa, the residence time of the liquid phase part in the viscosity breaking tower is 200 minutes, the viscosity breaking generated oil and the light gas oil are mixed and enter a fractionating tower to be fractionated, cracked gas and cracked gasoline are obtained at the top of the tower, and viscosity breaking residual oil is obtained at the bottom of the tower.
The toluene-insoluble matter (coke) content of the viscosity-reduced oil and light gas oil mixture was 0.00% (by mass). The viscosity-reducing conversion rate is 2.5%, and the kinematic viscosity of the viscosity-reduced residual oil at 100 ℃ is 155.3mm 2 And/s, the speckle test result of the viscosity-reduced residual oil is grade 1, the viscosity-reduced residual oil has good stability, and the viscosity-reduced residual oil has the stability less than grade 3.
Comparative example 2
Liaohe super heavy oil is used as raw oil, wherein the density of the raw oil at 20 ℃ is 1004.6kg/m 3 And a kinematic viscosity at 100 ℃ of 905.6mm 2 The carbon residue was 13.72wt%, and the content of fractions less than 165 ℃ and the content of residual oil more than 350 ℃ in the feed oil were 0.01wt% and 91.1wt%.
The experiment is carried out in a pilot-scale viscosity breaking device, raw oil is mixed with water, the mass ratio of the water to the raw oil is 0.3wt%, the mixture enters a heating unit, namely a heating furnace, to be heated, the temperature of a furnace outlet is 370 ℃, the heated material enters the viscosity breaking tower from the bottom of the viscosity breaking tower to be subjected to viscosity breaking, the viscosity breaking generated oil flows out of the top of the viscosity breaking tower, the pressure of the top of the viscosity breaking tower is 0.2MPa, the retention time of the material in the viscosity breaking tower is 200 minutes, the viscosity breaking generated oil enters a fractionating tower to be fractionated, cracked gas and cracked gasoline are obtained at the top of the tower, and viscosity breaking residual oil is obtained at the bottom of the tower.
The viscosity-reduced oil had a toluene-insoluble (coke) content of 0.18% (mass fraction), a viscosity-reduction conversion of 1.6%, and a kinematic viscosity of 204.7mm at 100 ℃ for the viscosity-reduced residue 2 And/s, the speckle test result of the viscosity-reduced residual oil is grade 2, the viscosity-reduced residual oil has good stability, and the viscosity-reduced residual oil has the stability less than grade 3.
Example 3
Liaohe super heavy oil is used as raw oil, wherein the density of the raw oil at 20 ℃ is 1004.6kg/m 3 And a kinematic viscosity at 100 ℃ of 905.6mm 2 The carbon residue was 13.72wt%, and the content of fractions less than 165 ℃ and the content of residual oil more than 350 ℃ in the feed oil were 0.01wt% and 91.1wt%.
The experiment is carried out in a pilot-scale viscosity breaking device, raw oil is mixed with water, the mass ratio of the water to the raw oil is 0.3wt%, the mixture enters a heating unit, namely a heating furnace, to be heated, the temperature of a furnace outlet is 375 ℃, the heated material enters a gas-liquid separation tank, after gas-liquid separation, the water and light gas oil are discharged from the top outlet of the gas-liquid separation unit, a liquid phase part flows out from the bottom outlet of the gas-liquid separation tank, enters the viscosity breaking tower from the bottom of the viscosity breaking tower to be subjected to viscosity breaking, viscosity breaking generated oil flows out from the top of the viscosity breaking tower, the pressure at the top of the viscosity breaking tower is 0.2MPa, the residence time of the liquid phase part in the viscosity breaking tower is 200 minutes, the viscosity breaking generated oil and the light gas oil are mixed and enter a fractionating tower to be fractionated, cracked gas and cracked gasoline are obtained at the top of the tower, and viscosity breaking residual oil is obtained at the bottom of the tower.
The toluene insoluble (coke) content of the visbreaking product oil and light gas oil mixed oil is 0.00 percent (mass fraction), the visbreaking conversion rate is 3.8 percent, and the kinematic viscosity of the visbreaking residual oil at 100 ℃ is 89.7mm 2 And/s, the speckle test result of the viscosity-reduced residual oil is grade 1, the viscosity-reduced residual oil has good stability, and the viscosity-reduced residual oil has the stability less than grade 3.
Example 4-1
Vacuum residue was used as the feed oil, wherein the density of the feed oil at 20 ℃ was 921.4kg/m 3 At 100 deg.CThe kinematic viscosity is 156.8mm 2 The carbon residue was 6.72wt%.
The experiment is carried out in a pilot-scale viscosity breaking device, raw oil and water are mixed, the mass ratio of the water to the raw oil is 1.8wt%, the mixture enters a heating unit, namely a heating furnace, to be heated, the temperature of a furnace outlet is 450 ℃, the heated material enters a gas-liquid separation tank, after gas-liquid separation, the water and light gas oil are discharged from the top outlet of the gas-liquid separation unit, a liquid phase part flows out from the bottom outlet of the gas-liquid separation tank, enters the viscosity breaking tower from the bottom of the viscosity breaking tower to be subjected to viscosity breaking, viscosity breaking generated oil flows out from the top of the viscosity breaking tower, the pressure at the top of the viscosity breaking tower is 0.5MPa, the residence time of the liquid phase part in the viscosity breaking tower is 20 minutes, the viscosity breaking generated oil and the light gas oil are mixed and enter a fractionating tower to be fractionated, cracked gas and cracked gasoline are obtained at the top of the tower, and viscosity breaking residual oil is obtained at the bottom of the tower.
The toluene insoluble (coke) content of the visbreaking product oil and light gas oil mixed oil is 0.00 percent (mass fraction), the visbreaking conversion rate is 5.8 percent, and the kinematic viscosity of the visbreaking residual oil at 100 ℃ is 35.2mm 2 And/s, the speckle test result of the viscosity-reduced residual oil is grade 1, the viscosity-reduced residual oil has good stability, and the viscosity-reduced residual oil has the stability less than grade 3.
Example 4 to 2
Vacuum residuum was used as feed oil, wherein the density of the feed oil at 20 ℃ was 921.4kg/m 3 A kinematic viscosity at 100 ℃ of 156.8mm 2 The carbon residue was 6.72wt%.
The experiment is carried out in a pilot-scale viscosity breaking device, raw oil and water are mixed, the mass ratio of the water to the raw oil is 1.8wt%, the mixture enters a heating unit, namely a heating furnace, to be heated, the temperature of a furnace outlet is 460 ℃, the heated material enters a gas-liquid separation tank, after gas-liquid separation, the water and light gas oil are discharged from the top outlet of the gas-liquid separation unit, a liquid phase part flows out from the bottom outlet of the gas-liquid separation tank, enters the viscosity breaking tower from the bottom of the viscosity breaking tower to be subjected to viscosity breaking, viscosity breaking generated oil flows out from the top of the viscosity breaking tower, the pressure at the top of the viscosity breaking tower is 0.5MPa, the residence time of the liquid phase part in the viscosity breaking tower is 20 minutes, the viscosity breaking generated oil and the light gas oil are mixed and enter a fractionating tower to be fractionated, cracked gas and cracked gasoline are obtained at the top of the tower, and viscosity breaking residual oil is obtained at the bottom of the tower.
The toluene insoluble (coke) content of the viscosity-reduced product oil and light gas oil mixed oil is 0.11% (mass fraction), the viscosity-reduction conversion rate is 7.2%, and the kinematic viscosity of the viscosity-reduced residual oil at 100 ℃ is 24.6mm 2 And/s, the speckle test result of the viscosity-reduced residual oil is grade 1, the stability of the viscosity-reduced residual oil is good, and the stability of the viscosity-reduced residual oil is less than the requirement of grade 3.
Comparative example 3
Vacuum residue was used as the feed oil, wherein the density of the feed oil at 20 ℃ was 921.4kg/m 3 A kinematic viscosity at 100 ℃ of 156.8mm 2 The carbon residue was 6.72wt%.
The experiment is carried out in a pilot-scale viscosity breaking device, raw oil is mixed with water, the mass ratio of the water to the raw oil is 1.8wt%, the mixture enters a heating unit, namely a heating furnace, to be heated, the temperature of a furnace outlet is 450 ℃, the heated material enters the viscosity breaking tower from the bottom of the viscosity breaking tower to be subjected to viscosity breaking, the viscosity breaking generated oil flows out from the top of the viscosity breaking tower, the pressure of the top of the viscosity breaking tower is 0.5MPa, the retention time of the material in the viscosity breaking tower is 20 minutes, the viscosity breaking generated oil and light gas oil are mixed and enter a fractionating tower to be fractionated, cracked gas and cracked gasoline are obtained at the top of the tower, and viscosity breaking residual oil is obtained at the bottom of the tower.
The toluene insoluble (coke) content of the viscosity-reduced product oil and light gas oil mixed oil is 0.17% (mass fraction), the viscosity-reduction conversion rate is 4.1%, and the kinematic viscosity of the viscosity-reduced residual oil at 100 ℃ is 54.8mm 2 And/s, the speckle test result of the viscosity-reduced residual oil is grade 2, the viscosity-reduced residual oil has good stability, and the viscosity-reduced residual oil has the stability less than grade 3.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
under the condition of using the visbreaking method and the visbreaking device, because the step of gas-liquid separation is carried out before the visbreaking reaction, water and light gas oil are effectively removed from raw oil, namely gas-phase components such as water and light gas oil which cause the maximum material back-mixing are removed, so that the visbreaking reaction is more uniform, the visbreaking temperature can be higher or the reaction time can be longer, and the visbreaking reaction depth can be increased. As can be seen from the comparison between the examples and the comparative examples, in the case of using the visbreaking method and the visbreaking apparatus of the present application, under the same visbreaking conditions as compared with the prior art, the coking rate of the visbroken produced oil is significantly reduced, the stability of the visbroken residue is good, the conversion rate is improved, the viscosity of the visbroken residue is smaller, that is, the visbreaking efficiency is improved; under the same condition of viscosity-reducing coking rate of the oil, the viscosity-reducing conversion rate is obviously improved.
The present invention has been described in terms of the preferred embodiment, and it is not intended to be limited to the embodiment. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (11)
1. A visbreaking apparatus, comprising:
a raw material supply unit including a raw material oil supply device (1) and a water supply device (2);
a heating unit (3) having a raw material inlet and a hot mixture outlet, the raw material inlet being connected to the raw material oil supply device (1) and the water supply device (2);
the gas-liquid separation unit (4) is provided with an inlet of a substance to be separated, an outlet of a gaseous substance to be separated and an outlet of a liquid substance to be separated, the inlet of the substance to be separated is connected with the outlet of the hot mixture, the gas-liquid separation unit (4) is used for carrying out gas-liquid separation on the hot mixture to obtain a gaseous substance to be separated and a liquid substance to be separated, and the gaseous substance to be separated comprises water and light gas oil; and
and the viscosity breaking unit (5) is connected with the liquid isolate outlet and is used for performing viscosity breaking reaction on the liquid isolate.
2. The visbreaking apparatus according to claim 1, wherein the visbreaking unit (5) comprises a visbreaking reaction tower having an inlet for the material to be cracked and an outlet for the visbroken product oil, the inlet for the material to be cracked is connected to the outlet for the liquid separated material, the inlet for the material to be cracked is disposed at the bottom of the visbreaking reaction tower, and the outlet for the visbroken product oil is disposed at the top of the visbreaking reaction tower.
3. The visbreaking apparatus of claim 2, further comprising:
and the fractionating equipment (6) is connected with the viscosity breaking and cracking generated oil outlet and is used for fractionating the viscosity breaking and cracking generated oil.
4. A visbreaking process, comprising:
step S1: heating a mixture comprising raw oil and water to obtain a hot mixture;
step S2: carrying out gas-liquid separation on the hot mixture to obtain a gaseous separator and a liquid separator, wherein the gaseous separator comprises water and light gas oil;
and step S3: and performing visbreaking on the liquid isolate to obtain visbroken produced oil.
5. The visbreaking process of claim 4, further comprising:
and S4, fractionating the visbreaking produced oil to obtain cracked gas, cracked gasoline and visbreaking residual oil.
6. The visbreaking method according to claim 4, wherein in the step S1, the mass ratio of the water to the feedstock oil is 0.3 to 1.8.
7. The visbreaking process according to claim 4, wherein in step S1 the temperature of the hot mixture is in the range of 370 ℃ to 460 ℃.
8. The visbreaking process of claim 4, wherein the visbreaking is carried out at an overhead pressure of from 0.2MPa to 0.7 MPa.
9. The visbreaking process of claim 4, wherein step S3 comprises subjecting the liquid isolate to a visbreaking reaction for 20 to 200 minutes.
10. The visbreaking process of claim 4, further comprising fractionating the gaseous isolate separated in step S2 together with the visbroken product oil in step S3.
11. The visbreaking process of claim 4, wherein the feed oil comprises extra heavy crude, atmospheric resid, vacuum resid, or deoiled bitumen.
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| CN202110639024.1A CN115449396A (en) | 2021-06-08 | 2021-06-08 | Visbreaking device and visbreaking method |
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