CN110218581B - Modification method of oil sand asphalt - Google Patents
Modification method of oil sand asphalt Download PDFInfo
- Publication number
- CN110218581B CN110218581B CN201810173337.0A CN201810173337A CN110218581B CN 110218581 B CN110218581 B CN 110218581B CN 201810173337 A CN201810173337 A CN 201810173337A CN 110218581 B CN110218581 B CN 110218581B
- Authority
- CN
- China
- Prior art keywords
- oil
- hydrotreating
- visbreaking
- oil sand
- sand asphalt
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a method for modifying oil sand asphalt, which comprises the following steps: and (3) performing viscosity breaking and hydrotreating on the oil sand asphalt to obtain an oil product meeting the pipeline transportation requirement. The modification method provided by the invention is simple to operate, can improve the effective product yield and increase the sales income, and the method for treating the oil sand asphalt has no residue discharge and meets the environmental protection requirement.
Description
Technical Field
The invention relates to a method for modifying oil sand asphalt, in particular to a method for modifying oil sand asphalt to ensure that the flow property of the oil sand asphalt meets the pipeline transportation requirement.
Background
The oil sand asphalt is essentially high-viscosity crude oil and has the characteristics of high density, high sulfur content, high asphaltene content, high metal Ni content, high metal V content and the like. Oil sand bitumen is very viscous and can hardly flow at normal temperature, and needs to be treated for transportation and utilization. For convenient transportation, the processing of oil sand bitumen is divided into bitumen dilution and bitumen upgrading. Asphalt dilution is to dilute unmodified asphalt by using light oil products such as condensate oil or naphtha and the like to obtain diluted asphalt, but the consumption of a diluent is about 66 percent of that of oil sand asphalt, the use of a large amount of high-value diluent occupies more mobile capital and is unreasonable economically, and meanwhile, a large amount of diluent also occupies valuable pipeline transportation space, so that the effective transportation amount of the oil sand asphalt is reduced. Asphalt modification is to process oil sand asphalt into various synthetic crude oils such as light low-sulfur, medium-sulfur and heavy-sulfur by means of coking (including delayed coking and fluid coking), solvent deasphalting, ebullated bed hydrogenation and the like in a modification plant, and the modification method needs higher treatment cost to solve the residue problem.
For example, chinese patent No. CN200510127799.1, entitled "a method for treating oil sands bitumen" discloses a method for processing oil sands bitumen by a combination of visbreaking and solvent deasphalting processes. Although the method can obtain higher yield of the synthetic crude oil, the olefin content in the product exceeds 1 percent, the product does not meet the pipeline transportation requirement, and the product cannot really enter a pipe network for transportation. There is no disclosure of a method for processing oil sand bitumen by a combined visbreaking and hydrotreating process to improve its pipeline transport properties and increase economic efficiency.
Disclosure of Invention
The technical problem to be solved by the application is to provide a method for upgrading oil sand asphalt, wherein the method can be used for upgrading the oil sand asphalt so that the flowing property of the oil sand asphalt meets the pipeline transportation requirement.
The term "oil sand bitumen" as used herein generally refers to oil sand bitumen that has been subjected to preliminary separation to remove minerals such as sand and clay after it has been mined by surface mining or by steam thermal mining techniques.
The term "oil product capable of pipeline transportation" as used herein refers to a material capable of pipeline transportation under the normal transportation conditions of the crude oil transportation art. Preferably, the oil capable of being conveyed by pipelines is oil with viscosity of less than 350mm at 8 DEG C2And/s, bromine number is less than or equal to 10g Br per 100g of material.
In order to solve the technical problems, the invention adopts the following technical scheme:
a method for upgrading oil sand bitumen comprises the following steps: and (3) performing viscosity breaking and hydrotreating on the oil sand asphalt to obtain an oil product meeting the pipeline transportation requirement.
As a further improvement of the technical scheme, the heavy components with boiling points of more than 500 ℃ generated by the visbreaking are subjected to a gasification process to obtain synthesis gas, and hydrogen used for the hydrotreating step is extracted from the synthesis gas; the hydrotreating comprises a hydrofining technology or a hydrocracking technology.
As a further improvement of the technical scheme, before visbreaking, oil sand asphalt is subjected to atmospheric distillation to separate a light component I, and then a heavy component I obtained by atmospheric distillation is subjected to visbreaking treatment.
Preferably, the division point of the light and heavy components of the atmospheric distillation is controlled between 200 ℃ and 400 ℃. More preferably, the division point of the light and heavy components of the atmospheric distillation is controlled between 350 ℃ and 400 ℃.
As a further improvement of the technical scheme, before hydrotreating, heavy component II is separated from a product obtained by visbreaking through a distillation unit, and then light component II obtained by the distillation unit is hydrotreated.
Preferably, the division point of the light and heavy components of the distillation unit is controlled between 500 ℃ and 560 ℃.
Preferably, the distillation unit may be an atmospheric distillation apparatus or a vacuum distillation apparatus.
As a further improvement of the technical scheme, the oil product capable of being transported by a pipe is prepared by blending all light components I, all products after hydrotreating and part of heavy components II, wherein the heavy components II in the oil product for transporting by a pipe account for 0-60% by mass, and the light components I and the products after hydrotreating account for the oil sand asphalt raw material by mass respectively; or blending all the light components I, all the products after hydrotreating and oil sand asphalt, wherein the oil sand asphalt accounts for 0-60% of the pipeline oil transportation product by mass, and the light components I and the products after hydrotreating are blended according to the mass yield of the oil sand asphalt raw material by mass respectively.
As a further improvement of the technical scheme, the heavy component II is prepared into synthesis gas through a gasification process, and hydrogen is extracted from the synthesis gas and used as hydrogen required by hydrotreatment.
As a further improvement of the technical scheme, the visbreaking reaction is preferably carried out under the conditions that the temperature is 350-450 ℃, the pressure is 0.05-15 MPa, and the retention time is 0.1-5 h. More preferably, the reaction is carried out at a temperature of 400 ℃ to 420 ℃, a pressure of 0.3MPa to 1MPa and a residence time of 0.5h to 1.5 h.
As a further improvement of the technical scheme, the hydrotreating process is preferably carried out at the temperature of 350-450 ℃, the pressure of 5-20 MPa and the space velocity of 0.5h-1-3h-1The hydrogen-oil ratio (v/v) is 500-3000. More preferably, the temperature is 360-380 ℃, the pressure is 12-15 MPa, and the space velocity is 1.0h-1-1.5h-1The hydrogen-oil ratio (v/v) is 800-1000.
Any range recited herein is intended to include the endpoints and any number between the endpoints and any subrange subsumed therein or defined therein.
The starting materials of the present invention are commercially available, unless otherwise specified, and the equipment used in the present invention may be any equipment conventionally used in the art or may be any equipment known in the art.
Compared with the prior art, the invention has the following beneficial effects:
the method of the invention has simple operation, can improve the effective product yield and increase the sales income. The mass yield of effective products of the existing widely applied modification technology is generally 60-65%, and the mass yield of the effective products of the method can reach 65-70%. The method for treating the oil sand asphalt has no residue discharge and meets the requirement of environmental protection.
Drawings
FIG. 1 is a process flow diagram of a process for upgrading oil sands bitumen as provided in example 1 of the present invention;
FIG. 2 is a process flow diagram of a method for upgrading oil sand bitumen as provided in example 2 of the present invention.
Detailed Description
In order to more clearly illustrate the invention, the invention is further described below in connection with preferred embodiments. It is to be understood by persons skilled in the art that the following detailed description is illustrative and not restrictive, and is not to be taken as limiting the scope of the invention.
The invention relates to a method for modifying oil sand asphalt, which comprises the following steps: and (3) performing viscosity breaking and hydrotreating on the oil sand asphalt to obtain an oil product meeting the pipeline transportation requirement.
Research shows that oil products meeting the pipeline transportation requirements can be obtained by carrying out visbreaking and hydrotreating on the oil sand asphalt.
According to certain embodiments of the present application, the heavy components produced by said visbreaking and having a boiling point >500 ℃ are subjected to a gasification process to obtain synthesis gas, and hydrogen is extracted from the synthesis gas for the hydrotreating step; the hydrotreating comprises a hydrofining technology or a hydrocracking technology.
According to certain embodiments of the present application, prior to visbreaking, oil sand bitumen is subjected to atmospheric distillation to separate a light fraction I, and the heavy fraction I obtained from atmospheric distillation is subjected to visbreaking. The light component I obtained by atmospheric distillation can be directly used as an oil product for pipeline transportation, and can also be blended with other components to obtain an oil product meeting the pipeline transportation requirement; at the same time, this step can reduce the load of visbreaking.
According to certain preferred embodiments of the present application, the cut point of the atmospheric distillation light and heavy components is controlled between 200 ℃ and 400 ℃. More preferably, the division point of the light and heavy components of the atmospheric distillation is controlled between 350 ℃ and 400 ℃.
According to certain embodiments of the present application, before the hydrotreating, the products obtained from the visbreaking are subjected to a distillation unit to separate heavy fraction II, and the light fraction II obtained from said distillation unit is subjected to a hydrotreating process. The product obtained by hydrotreating can be directly used as an oil product for pipeline transportation, and can also be blended with other components to obtain the oil product meeting the pipeline transportation requirement.
According to certain preferred embodiments of the present application, the cut point of the light and heavy components of the distillation unit is controlled between 500 ℃ and 560 ℃.
According to certain preferred embodiments of the present application, the distillation unit may be an atmospheric distillation apparatus or a vacuum distillation apparatus.
According to certain embodiments of the present application, the oil capable of being piped is blended with all of the light fraction I, all of the hydrotreated product, and a portion of the heavy fraction II; or blended from all light components I, all hydrotreated products and oil sand bitumen.
According to certain embodiments of the present application, heavy component II is made into syngas by a gasification process, and hydrogen is extracted from the syngas as hydrogen needed for hydroprocessing.
In accordance with certain embodiments of the present application, visbreaking refers to a mild thermal cracking process primarily to minimize the viscosity of the material and improve the pipe transport properties of oil sands bitumen. The reduction in viscosity is achieved primarily by thermal cracking of the non-asphaltenes. Visbreaking is a well-established heavy oil upgrading process, which is well known to those skilled in the art, and the conditions of visbreaking are not particularly limited in the present invention and can be carried out under various reasonable temperature and pressure conditions. In the specific embodiment of the invention, the visbreaking reaction is preferably carried out at a temperature of 350-450 ℃, a pressure of 0.05-15 MPa and a residence time of 0.1-5 h. More preferably, the reaction is carried out at a temperature of 400 ℃ to 420 ℃, a pressure of 0.3MPa to 1MPa and a residence time of 0.5h to 1.5 h. The specific operation of such visbreaking is well known to those skilled in the art and will not be described herein.
The hydrogenation treatment of the invention can adopt hydrofining technology or hydrocracking technology, and mainly aims to saturate olefins in oil products and further reduce the viscosity of materials. Both hydrofinishing and hydrocracking are well known to those skilled in the art, and the present invention is not particularly limited to the conditions of the hydrotreating process and can be carried out under various reasonable conditions. In the specific embodiment of the invention, the hydrotreating process is preferably carried out at the temperature of 350-450 ℃, the pressure of 5-20 MPa and the space velocity of 0.5h-1-3h-1The hydrogen-oil ratio (v/v) is 500-3000. More preferably, the temperature is 360-380 ℃, the pressure is 12-15 MPa, and the space velocity is 1.0h-1-1.5h-1The hydrogen-oil ratio (v/v) is 800-1000. The specific operation of such hydrotreating is well known to those skilled in the art and will not be described herein.
The following examples further illustrate the invention. The oil sand bitumen used in the examples of the present invention was SAGD produced oil sand bitumen from Nexen, and its main properties are shown in Table 1.
Example 1
According to the process shown in figure 1, the method for upgrading oil sand bitumen comprises the following steps:
feeding oil sand asphalt into an atmospheric distillation unit, directly separating distillate oil with a boiling point lower than 350 ℃ in the oil sand asphalt as a component capable of being conveyed by a pipeline, and feeding the residual high-boiling distillation residual oil into a viscosity breaking unit for viscosity breaking under the conditions of 415 ℃ of temperature, 0.5MPa of pressure and 50min of retention time. And (3) separating the products after visbreaking in a distillation unit, separating out components with the boiling point lower than 520 ℃ to be used as a raw material for hydrotreating, using one part of the rest high-boiling heavy components as a blending component of the oil product for pipeline transportation, and using the other part of the rest high-boiling heavy components as a gasification raw material. The hydrogenation process adopts hydrofining technology, and the conditions are that the temperature is 360 ℃, the pressure is 15MPa, and the space velocity is 1.2h-1The hydrogen-oil ratio (v/v) was 900. The obtained oil for pipe transportation is obtained in the above steps<350 deg.C fraction oil, hydrorefiningThe back distillate oil and part of distillation heavy components are blended, and the blending ratio is (by mass):<10.17% of distillate 350, 41.83% of distillate after hydrocracking and 48% of distillation heavy components, and the results of property analysis are shown in Table 1.
Example 2
Referring to FIG. 2, the method for upgrading oil sand bitumen comprises the following steps:
feeding oil sand asphalt into an atmospheric distillation unit, directly separating components with the boiling point lower than 350 ℃ in the oil sand asphalt as components capable of being conveyed by a pipeline, and feeding the residual high-boiling-point distillation residual oil into a viscosity breaking unit for viscosity breaking under the conditions of 410 ℃ of temperature, 0.5MPa of pressure and 50min of retention time. And (3) separating the products after visbreaking in a distillation unit, separating out components with the boiling point lower than 535 ℃ to be used as a raw material for hydrotreating, and using the rest high-boiling-point heavy components as gasification raw materials. The hydrotreating process adopts hydrocracking technology, and has the conditions of 370 deg.c temperature, 15MPa pressure and 1.5 hr space velocity-1The hydrogen-oil ratio (v/v) was 900. The obtained oil for pipe transportation is obtained in the above steps<The distillate oil with the temperature of 350 ℃, the distillate oil after hydrocracking and the oil sand asphalt are blended, and the blending ratio is (by mass fraction):<9.71 percent of distillate 350, 37.29 percent of distillate after hydrocracking and 53 percent of oil sand bitumen, and the results of the property analysis are shown in Table 1.
TABLE 1 Properties of the feedstock and the oil conveyed in a pipe
It should be understood that the above-described embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. Not all embodiments are exhaustive. All obvious changes and modifications which are obvious to the technical scheme of the invention are covered by the protection scope of the invention.
Claims (8)
1. A method for modifying oil sand asphalt is characterized by comprising the following steps: performing visbreaking and hydrotreating on the oil sand asphalt;
before visbreaking, oil sand asphalt is subjected to atmospheric distillation to separate a light component I, and then a heavy component I obtained by atmospheric distillation is subjected to visbreaking treatment; the division point of the light and heavy components in the atmospheric distillation is controlled between 200 ℃ and 400 ℃;
before hydrotreating, separating heavy component II from the product obtained by visbreaking through a distillation unit, and hydrotreating the light component II obtained by the distillation unit; the division point of the light and heavy components of the distillation unit is controlled between 500 ℃ and 560 ℃; preparing the heavy component II into synthesis gas through a gasification process, and extracting hydrogen from the synthesis gas to be used as hydrogen required by hydrotreating;
the oil product capable of being conveyed by a pipeline is formed by blending all light components I, all products after hydrotreating and part of heavy components II, the heavy components II in the oil product for pipeline conveyance account for 0-60% by mass, and the light components I and the products after hydrotreating account for the oil sand asphalt raw material respectively in mass yield; or blending all the light component I, all the hydrotreated products and oil sand asphalt, wherein the oil sand asphalt accounts for 0-60% by mass of the oil product for pipeline transportation, and the light component I and the hydrotreated products are blended according to the mass yield of the oil sand asphalt raw material respectively, so as to obtain the oil product capable of being conveyed by a pipeline;
the oil product capable of being conveyed by a pipeline has viscosity of less than 350mm at 8 DEG C2And/s, bromine number is less than or equal to 10g Br per 100g of material.
2. The process for upgrading bitumen from oil sands according to claim 1, characterized in that: obtaining synthesis gas from heavy components with boiling points of more than 500 ℃ generated by visbreaking through a gasification process, and extracting hydrogen used for the hydrotreating step from the synthesis gas; the hydrotreating comprises a hydrofining technology or a hydrocracking technology.
3. The process for upgrading bitumen from oil sands according to claim 1, characterized in that: the division point of the light and heavy components in the atmospheric distillation is controlled between 350 ℃ and 400 ℃.
4. The process for upgrading bitumen from oil sands according to claim 1, characterized in that: the distillation unit is an atmospheric distillation device or a reduced pressure distillation device.
5. The process for upgrading bitumen from oil sands according to claim 1, characterized in that: the visbreaking reaction is carried out under the conditions that the temperature is 350-450 ℃, the pressure is 0.05-15 MPa, and the retention time is 0.1-5 h.
6. The process for upgrading bitumen oil sands according to claim 5, characterized in that: the visbreaking reaction is carried out at the temperature of 400-420 ℃, under the pressure of 0.3-1 MPa and for the residence time of 0.5-1.5 h.
7. The process for upgrading bitumen from oil sands according to claim 1, characterized in that: the hydrotreating process is carried out at 350-450 deg.C, 5-20 MPa and 0.5h airspeed-1-3h-1The hydrogen-oil ratio v/v is 500-3000.
8. The process for upgrading bitumen oil sands according to claim 7, characterized in that: the hydrotreating process is carried out at the temperature of 360-380 ℃, the pressure of 12-15 MPa and the airspeed of 1.0h-1-1.5h-1The hydrogen-oil ratio v/v is 800-1000.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810173337.0A CN110218581B (en) | 2018-03-02 | 2018-03-02 | Modification method of oil sand asphalt |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810173337.0A CN110218581B (en) | 2018-03-02 | 2018-03-02 | Modification method of oil sand asphalt |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110218581A CN110218581A (en) | 2019-09-10 |
| CN110218581B true CN110218581B (en) | 2021-07-20 |
Family
ID=67822037
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810173337.0A Active CN110218581B (en) | 2018-03-02 | 2018-03-02 | Modification method of oil sand asphalt |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110218581B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113088329B (en) * | 2019-12-23 | 2023-02-24 | 中国石油天然气股份有限公司 | Method and device for viscosity reduction and modification of inferior heavy oil |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1351125A (en) * | 2000-10-26 | 2002-05-29 | 中国石油化工股份有限公司 | Hydrogenating process for reducing viscosity of heavy oil or residual oil |
| CN1775909A (en) * | 2005-12-07 | 2006-05-24 | 中国海洋石油总公司 | Oil sand asphalt treating method |
| CN103102934A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Pretreatment method for inferior heavy oil |
| CN103102984A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Hydrogenation combined process for inferior heavy oil |
| CN106753509A (en) * | 2016-11-24 | 2017-05-31 | 辽宁石油化工大学 | A kind of oil sands bitumen blends the visbreaking processing method of dead oil |
-
2018
- 2018-03-02 CN CN201810173337.0A patent/CN110218581B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1351125A (en) * | 2000-10-26 | 2002-05-29 | 中国石油化工股份有限公司 | Hydrogenating process for reducing viscosity of heavy oil or residual oil |
| CN1775909A (en) * | 2005-12-07 | 2006-05-24 | 中国海洋石油总公司 | Oil sand asphalt treating method |
| CN103102934A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Pretreatment method for inferior heavy oil |
| CN103102984A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Hydrogenation combined process for inferior heavy oil |
| CN106753509A (en) * | 2016-11-24 | 2017-05-31 | 辽宁石油化工大学 | A kind of oil sands bitumen blends the visbreaking processing method of dead oil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110218581A (en) | 2019-09-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8821712B2 (en) | Process for treating a heavy hydrocarbon feedstock and a product obtained therefrom | |
| CA2867914C (en) | Integration of solvent deasphalting with resin hydroprocessing and with delayed coking | |
| US9273256B2 (en) | Increased production of fuels by integration of vacuum distillation with solvent deasphalting | |
| CN103987813B (en) | The integration that solvent deasphalting processes with adding hydrogen into resin | |
| TW201538707A (en) | Process for refining a heavy hydrocarbon-containing feedstock implementing a selective cascade deasphalting | |
| US20150376513A1 (en) | Methods and apparatuses for hydrocracking and hydrotreating hydrocarbon streams | |
| CN110218581B (en) | Modification method of oil sand asphalt | |
| CA2479008A1 (en) | Method and facility for refining oil | |
| US9637686B2 (en) | Process for treating mined oil sands deposits | |
| CA2848789C (en) | Process for treating mined oil sands deposits | |
| CN107267199B (en) | The system and method for flash zone diesel oil for external process from delay coking process | |
| CN111100709A (en) | Method for producing high-value chemical products by adopting inferior LCO | |
| CN106147837B (en) | A kind of method of heavy oil modification viscosity reduction and application | |
| RU2625160C2 (en) | Method for improving heavy hydrocarbon mixture quality | |
| CA2526955C (en) | Process for treating a heavy hydrocarbon feedstock and a product obtained therefrom | |
| CN115678601A (en) | Hydrogenation-free upgrading process for heavy crude oil | |
| CN102816595B (en) | Residuum hydrotreatment-catalytic cracking combination technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |