Method and device for producing gasoline blend oil by taking light diesel oil as raw material

Abstract

The invention relates to the technical field of gasoline processing, and in particular relates to a method and a device for producing gasoline blend oil by taking light diesel oil as a raw material, the method comprises the following steps: 1, mixing the raw materials light diesel oil, etherified heavy gasoline and hydrogen, feeding into a hydro-upgrading unit, and carrying out hydro-upgrading reaction under the action of a hydro-upgrading catalyst, a hydro-upgrading reaction product is obtained; 2, the hydro-upgrading reaction product enters a hydrofining unit and is subjected to a hydrofining reaction under the action of a hydrofining catalyst, and a hydrofining reaction product is obtained; and 3, feeding the hydrofining reaction product into a rectification unit, and carrying out rectification separation to obtain condensed oil and product gasoline blending component oil. According to the invention, the light diesel oil, hydrogen and etherified heavy gasoline are mixed for hydro-upgrading and hydrofining treatment to obtain the product gasoline blending component oil, so that the octane number of the light diesel oil is effectively increased, the yield of the basic gasoline component is increased, the economic benefit is higher, and the processing route of the light diesel oil is widened.

Description

Technical Field

[0001] The invention relates to the technical field of gasoline processing, and is a method and a device for producing gasoline blending oil by taking light diesel as raw material. Background Art

[0002] The light diesel oil at the bottom of the tower, a byproduct of the hydrocarbon restructuring unit or diesel hydrotreating unit (under the naphtha processing scheme), has a distillation range of 135°C to 235°C. Compared with the refined diesel oil from the diesel hydrotreating unit, the light diesel oil has a lower flash point and a lower cetane number. From the perspective of the distillation range components, it is a component between gasoline and diesel. Compared with catalytic cracking heavy gasoline, the light diesel oil has a higher aromatic content, a lower olefin content, and a long-chain olefin molecule, and an octane number that is about 8 to 9 units lower. Compared with raffinate oil, the light diesel oil has a higher density and an octane number that is 9 to 10 units higher.

[0003] At present, the treatment route for light diesel is: entering the diesel blending pool and participating in diesel blending. Because light diesel has a low flash point and a low cetane number, a large amount of high flash point and high cetane number diesel is needed for diesel blending, which wastes a large amount of high-quality diesel. The treatment route for light diesel is relatively simple.

[0004] To solve this problem, some refineries have changed light diesel back to diesel hydrogenation units as raw materials, carried out hydrogenation refining reaction in the reaction stage, and then entered the fractionation tower for fractionation, and cut the light diesel into naphtha and diesel components again, thereby changing the flash point of diesel. The reprocessing of light diesel has increased the processing cost, and the diesel yield after processing has been reduced to about 50%, and 50% has been converted into naphtha components. The entire processing process has not increased high value-added products, and has not achieved quality improvement and efficiency increase. Summary of the invention

[0005] The present invention provides a method and device for producing gasoline blending oil using light diesel as raw material, which overcomes the shortcomings of the above-mentioned prior art and can effectively solve the problems of relatively single post-processing route and high processing cost of the existing light diesel.

[0006] One of the technical solutions of the present invention is achieved by the following measures: A method for producing gasoline blending oil using light diesel as raw material is carried out according to the following steps: In the first step, the raw materials of light diesel, etherified heavy gasoline and hydrogen are mixed and then enter the hydro-reforming unit, and the hydro-reforming reaction is carried out under the action of the hydro-reforming catalyst to obtain the hydro-reforming reaction product; In the second step, the hydro-refining reaction product enters the hydro-refining unit, and undergoes a hydro-refining reaction under the action of a hydro-refining catalyst to obtain a hydro-refining reaction product; In the third step, the hydrotreating reaction product enters the distillation unit for distillation separation to obtain condensate oil and product gasoline blending component oil.

[0007] The following is a further optimization and / or improvement of one of the above-mentioned technical solutions: In the first step, the feed ratio of light diesel and etherified heavy gasoline is 4 to 9:40, and the circulating hydrogen amount in hydrogen is 19500Nm 3 / h to 20500Nm 3 / h, the amount of new hydrogen is 1400Nm 3 / h to 1600Nm 3 / h.

[0008] In the first step above, the light diesel in the raw material is a by-product of the hydrocarbon restructuring unit or the diesel hydrogenation unit (under the naphtha processing scheme). The distillation range of light diesel is 135℃ to 235℃, the flash point is less than 62℃, and the density is 803Kg / m 3 Up to 809Kg / m 3 .

[0009] In the first step above, the etherified heavy gasoline in the raw material is the bottom product of the raw material cutting tower of the gasoline etherification unit, with a distillation range of 80°C to 196°C, and is a heavy component of catalytic cracking gasoline.

[0010] In the first step, the hydrogenation catalyst is a Ni / Zn molecular sieve structure, and the catalyst model is Fo-35m. The Fo-35m catalyst used in the present invention is developed and produced by PetroChina Fushun Petrochemical Company.

[0011] In the first step, the process conditions of hydro-upgrading are: reaction pressure 2.4MPa to 2.55MPa (G), volume hydrogen-to-oil ratio 240 to 250, and reaction inlet temperature 380°C to 390°C. Preferably, the reaction pressure of the hydro-upgrading unit is 2.5MPa (G), the reaction inlet temperature is 384°C, and the volume hydrogen-to-oil ratio is 245.

[0012] In the second step, the hydrotreating catalyst is a Co / Mo-alumina supported structure, and the catalyst model is PHG-111.

[0013] In the above second step, the process conditions of hydrofining are reaction pressure of 2.0 MPa to 2.4 MPa (G), reaction inlet temperature of 245°C to 280°C, and reaction outlet temperature of 285°C to 340°C. Preferably, the reaction pressure of the hydrofining unit is 2.1 MPa (G), the reaction inlet temperature is 262°C, and the reaction outlet temperature is 320°C.

[0014] The process conditions of the above-mentioned distillation unit are: the bottom temperature of the distillation tower is 180°C to 220°C, the top temperature is 85°C to 140°C, the top operating pressure is 0.7MPa to 1.0MPa, the top of the distillation tower obtains the separated product condensed oil, and the bottom of the tower obtains the product gasoline blending component oil. Preferably, the bottom temperature of the distillation unit is 185°C, the top temperature is 105°C, and the top operating pressure is 0.76MPa.

[0015] The second technical solution of the present invention is achieved by the following measures: a device for implementing a method for producing gasoline blending oil using light diesel as raw material, comprising a hydrogenation reforming unit, a hydrofining unit and a distillation unit, the distillation unit comprising a distillation tower, an air cooler, a circulating water cooler and a tower top reflux tank, the feed end of the hydrogenation reforming unit is fixedly connected with a raw material pipeline, the feed end of the raw material pipeline is fixedly connected with a light diesel pipeline, a hydrogen pipeline and an etherified heavy gasoline pipeline, the discharge end of the hydrogenation reforming unit and the feed end of the hydrofining unit are fixedly connected with a degassing pipeline, and the feed end of the hydrofining unit is fixedly connected with a degassing pipeline. A de-distillation pipeline is fixedly connected between the discharge end of the hydrorefining unit and the first feed end of the distillation tower, a first cooling pipeline is fixedly connected between the top discharge end of the distillation tower and the feed end of the air cooler, a second cooling pipeline is fixedly connected between the discharge end of the air cooler and the feed end of the circulating water cooler, a third cooling pipeline is fixedly connected between the discharge end of the circulating water cooler and the feed end of the top reflux tank, a condensed oil pipeline is fixedly connected to the discharge end of the top reflux tank, and a product gasoline blending component oil pipeline is fixedly connected to the bottom discharge end of the distillation tower.

[0016] The following is a further optimization and / or improvement of the second technical solution of the above invention: A reflux pipeline is fixedly connected between the condensed oil pipeline and the second feed end of the distillation tower.

[0017] The present invention provides a method and device for producing gasoline blending oil with light diesel as raw material. The method comprises mixing light diesel, hydrogen and etherified heavy gasoline, and performing hydrogenation modification and hydrofining treatment on the obtained mixture to obtain a gasoline blending component oil product, which effectively increases the octane number of light diesel, improves the output of basic gasoline components, has low investment and operation costs, has high economic benefits, and broadens the processing route of light diesel. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Attached Figure 1 This is a schematic diagram of the process flow of Example 10 of the present invention.

[0019] The codes in the attached drawings are: 1 is a hydrogenation reforming unit, 2 is a hydrorefining unit, 3 is a distillation tower, 4 is an air cooler, 5 is a circulating water cooler, 6 is a tower top reflux tank, 7 is a raw material pipeline, 8 is a light diesel pipeline, 9 is a hydrogen pipeline, 10 is an etherification heavy gasoline pipeline, 11 is a dehydrorefining pipeline, 12 is a de-distillation pipeline, 13 is a first cooling pipeline, 14 is a second cooling pipeline, 15 is a third cooling pipeline, 16 is a reflux pipeline, 17 is a condensed oil pipeline, and 18 is a product gasoline blending component oil pipeline. DETAILED DESCRIPTION

[0020] The present invention is not limited by the following embodiments, and the specific implementation method can be determined according to the technical scheme of the present invention and the actual situation. Unless otherwise specified, the various chemical reagents and chemicals mentioned in the present invention are all known and commonly used chemical reagents and chemicals in the prior art. Normal temperature and room temperature in the present invention generally refer to a temperature of 15°C to 25°C, and are generally defined as 25°C.

[0021] In the present invention, unless otherwise specified, the equipment and devices used are all the equipment and devices known and used in the art.

[0022] The present invention will be further described below in conjunction with embodiments: Example 1: Figure 1 As shown, the method for producing gasoline blending oil using light diesel as raw material is carried out according to the following steps: In the first step, the raw materials of light diesel, etherified heavy gasoline and hydrogen are mixed and then enter the hydro-reforming unit 1, and a hydro-reforming reaction is carried out under the action of a hydro-reforming catalyst to obtain a hydro-reforming reaction product; In the second step, the hydro-refining reaction product enters the hydro-refining unit 2, and undergoes a hydro-refining reaction under the action of a hydro-refining catalyst to obtain a hydro-refining reaction product; In the third step, the hydrotreating reaction product enters the distillation unit for distillation separation to obtain condensate oil and product gasoline blending component oil.

[0023] Example 2: As an optimization of the above example, in the first step, the feed ratio of light diesel oil to etherified heavy gasoline is 4 to 9:40, and the circulating hydrogen amount in the hydrogen is 19500 Nm 3 / h to 20500Nm 3 / h, the amount of new hydrogen is 1400Nm 3 / h to 1600Nm 3 / h.

[0024] Example 3: As an optimization of the above example, in the first step, the light diesel in the raw material is a by-product of a hydrocarbon recombination unit or a diesel hydrogenation unit (under the naphtha processing scheme), and the distillation range of the light diesel is 135°C to 235°C, the flash point is less than 62°C, and the density is 803Kg / m3 Up to 809Kg / m 3 The main properties of the light diesel oil used in the present invention are shown in Table 1.

[0025] Example 4: As an optimization of the above example, in the first step, the etherified heavy gasoline in the raw material is the bottom product of the raw material cutting tower of the gasoline etherification unit, with a distillation range of 80°C to 196°C, and is a heavy component of catalytic cracking gasoline.

[0026] Example 5: As an optimization of the above example, in the first step, the hydrogenation reforming catalyst is a Ni / Zn molecular sieve structure, and the catalyst model is Fo-35m. The Fo-35m catalyst used in the present invention is developed and produced by PetroChina Fushun Petrochemical Company.

[0027] Example 6: As an optimization of the above example, in the first step, the process conditions of hydro-upgrading are: reaction pressure 2.4MPa to 2.55MPa (G), volume hydrogen-to-oil ratio 240 to 250, and reaction inlet temperature 380°C to 390°C. Preferably, the reaction pressure of the hydro-upgrading unit 1 is 2.5MPa (G), the reaction inlet temperature is 384°C, and the volume hydrogen-to-oil ratio is 245.

[0028] Example 7: As an optimization of the above example, in the second step, the hydrotreating catalyst is a Co / Mo-alumina supported structure, and the catalyst model is PHG-111.

[0029] Embodiment 8: As an optimization of the above embodiment, in the second step, the process conditions of hydrofining are reaction pressure 2.0MPa to 2.4MPa (G), reaction inlet temperature 245°C to 280°C, and reaction outlet temperature 285°C to 340°C. Preferably, the reaction pressure of the hydrofining unit 2 is 2.1MPa (G), the reaction inlet temperature is 262°C, and the reaction outlet temperature is 320°C.

[0030] Embodiment 9: As an optimization of the above embodiment, the process conditions of the distillation unit are: the bottom temperature of the distillation tower 3 is 180°C to 220°C, the top temperature is 85°C to 140°C, the top operating pressure is 0.7MPa to 1.0MPa, and the separated product condensed oil is obtained at the top of the distillation tower 3 and the separated product product gasoline blending component oil is obtained at the bottom of the tower. Preferably, the bottom temperature of the distillation unit is 185°C, the top temperature is 105°C, and the top operating pressure is 0.76MPa.

[0031] Example 10: Figure 1As shown, the device for implementing the method of producing gasoline blending oil using light diesel as raw material comprises a hydro-modification unit 1, a hydro-refining unit 2 and a distillation unit, wherein the distillation unit comprises a distillation tower 3, an air cooler 4, a circulating water cooler 5 and a tower top reflux tank 6, the feed end of the hydro-modification unit 1 is fixedly connected with a raw material pipeline 7, the feed end of the raw material pipeline 7 is fixedly connected with a light diesel pipeline 8, a hydrogen pipeline 9 and an etherified heavy gasoline pipeline 10, the discharge end of the hydro-modification unit 1 and the feed end of the hydro-refining unit 2 are fixedly connected with a dehydro-refining pipeline 11, and the hydro-refining unit 2 is fixedly connected with a dehydro-refining pipeline 11. A de-distillation pipeline 12 is fixedly connected between the discharge end and the first feed end of the distillation tower 3, a first cooling pipeline 13 is fixedly connected between the top discharge end of the distillation tower 3 and the feed end of the air cooler 4, a second cooling pipeline 14 is fixedly connected between the discharge end of the air cooler 4 and the feed end of the circulating water cooler 5, a third cooling pipeline 15 is fixedly connected between the discharge end of the circulating water cooler 5 and the feed end of the tower top reflux tank 6, a condensed oil pipeline 17 is fixedly connected to the discharge end of the tower top reflux tank 6, and a product gasoline blending component oil pipeline 18 is fixedly connected to the bottom discharge end of the distillation tower 3.

[0032] Example 11: Figure 1 As shown, as an optimization of the above embodiment, a reflux pipeline 16 is fixedly connected between the condensed oil pipeline 17 and the second feed end of the distillation tower 3. Part of the condensed oil is refluxed to the distillation tower 3 through the reflux pipeline 16.

[0033] As required, valves and instruments are fixedly installed on each pipeline of the device for producing gasoline blending oil using light diesel as raw material to enable normal operation. The hydro-reforming unit 1, the hydro-refining unit 2 and the distillation unit all use existing reactors and equipment, and the distillation tower 3 is a tray-type distillation tower 3.

[0034] The present invention mixes light diesel oil, hydrogen and etherified heavy gasoline, and performs hydrogenation and hydrorefining treatment on the obtained mixture to obtain product gasoline blending component oil. After the light diesel oil, hydrogen and etherified heavy gasoline are mixed, they enter the hydrogenation and reforming unit 1 to perform hydrogenation and reforming reaction, and perform hydrocracking, isomerization, aromatization, cyclization and other reactions in a fixed bed reactor, which can shorten the molecular carbon chain and improve the octane number of the light diesel oil. The obtained reaction product enters the hydrorefining unit 2 to perform hydrorefining reaction, and performs hydrodesulfurization and olefin saturation reaction in a fixed bed reactor. The reaction product of the hydrorefining reaction is separated by distillation to obtain condensed oil and product gasoline blending component oil. The product gasoline blending component oil enters the base gasoline blending pool, which increases the density of the base gasoline component, reduces the olefins of the base gasoline, and can reduce the transfer of high-density component oil.

[0035] Example 12: The gasoline blending oil produced using light diesel as raw material is produced according to the following process steps: The octane number of the light diesel in the raw material was determined to be 80.5, the feed rate of etherified heavy gasoline was 40t / h, the feed rate of light diesel was 8t / h, and the circulating hydrogen volume in the hydrogen was 20000Nm 3 / h, the amount of new hydrogen is 1500Nm 3 / h, In the first step, light diesel, etherified heavy gasoline and hydrogen are mixed and then enter the hydro-reforming unit 1 for hydro-reforming reaction. The inlet temperature of the hydro-reforming unit 1 is 384°C, the bed temperature drop is -13°C, the reaction pressure is 2.5MPa (G), the volume hydrogen-oil ratio is 245, and the hydro-reforming catalyst is Fo-35m catalyst to obtain a hydro-reforming reaction product; In the second step, the hydrorefining reaction product enters the hydrorefining unit 2 for hydrorefining reaction. The inlet temperature of the hydrorefining unit 2 is 265°C, the outlet temperature is 320°C, the reaction pressure is 2.1MPa (G), and the hydrorefining catalyst is PHG-111 catalyst to obtain a hydrorefining reaction product. In the third step, the hydrotreating reaction product enters the distillation unit. The top pressure of distillation tower 3 is 0.76 MPa, the bottom temperature is 185°C, and the top temperature is 105°C. The condensed oil and the product gasoline blending component oil are separated by distillation.

[0036] It has been determined that the octane number of light diesel after hydrogenation modification and hydrofining treatment is 82.0, an increase of 1.5 octane units, and the octane number of the product gasoline blending component oil is 86.6.

[0037] Example 13: The gasoline blending oil produced using light diesel as raw material is produced according to the following process steps: The octane number of the light diesel in the raw material was determined to be 80.5, the feed rate of etherified heavy gasoline was 40t / h, the feed rate of light diesel was 5t / h, and the circulating hydrogen volume in the hydrogen was 20000Nm 3 / h, the amount of new hydrogen is 1500Nm 3 / h; In the first step, light diesel, etherified heavy gasoline and hydrogen are mixed and then enter the hydro-reforming unit 1 for hydro-reforming reaction. The inlet temperature of the hydro-reforming unit 1 is 384°C, the bed temperature drop is -13°C, the reaction pressure is 2.5MPa (G), the volume hydrogen-to-oil ratio is 245, and the catalyst volume space velocity is 1.0h -1 , the hydro-reforming catalyst is Fo-35m catalyst, and a hydro-reforming reaction product is obtained; In the second step, the hydrorefining reaction product enters the hydrorefining unit 2 for hydrorefining reaction. The inlet temperature of the hydrorefining unit 2 is 265°C, the outlet temperature is 320°C, the reaction pressure is 2.1MPa (G), and the hydrorefining catalyst is PHG-111 catalyst to obtain a hydrorefining reaction product. In the third step, the hydrotreating reaction product enters the distillation unit. The top pressure of the distillation tower 3 is 0.76MPa, the bottom temperature is 185°C, and the top temperature is 105°C. The condensed oil and the product gasoline blending component oil are separated by distillation.

[0038] It has been determined that the octane number of light diesel after hydrogenation modification and hydrofining treatment is 81.6, an increase of 1.1 octane units, and the octane number of the product gasoline blending component oil is 86.5.

[0039] Example 14: The gasoline blending oil produced using light diesel as raw material is produced according to the following process steps: The octane number of the light diesel in the raw material was determined to be 80.5, the feed rate of etherified heavy gasoline was 40t / h, the feed rate of light diesel was 10t / h, and the circulating hydrogen amount in the hydrogen was 20000Nm 3 / h, the amount of new hydrogen is 1500Nm 3 / h; In the first step, light diesel, etherified heavy gasoline and hydrogen are mixed and then enter the hydro-reforming unit 1 for hydro-reforming reaction. The inlet temperature of the hydro-reforming unit 1 is 384°C, the bed temperature drop is -13°C, the reaction pressure is 2.5MPa (G), the volume hydrogen-to-oil ratio is 245, and the catalyst volume space velocity is 1.0h -1 , the hydro-reforming catalyst is Fo-35m catalyst, and a hydro-reforming reaction product is obtained; In the second step, the hydrorefining reaction product enters the hydrorefining unit 2 for hydrorefining reaction. The inlet temperature of the hydrorefining unit 2 is 265°C, the outlet temperature is 320°C, the reaction pressure is 2.1MPa (G), and the hydrorefining catalyst is PHG-111 catalyst to obtain a hydrorefining reaction product. In the third step, the hydrotreating reaction product enters the distillation unit. The top pressure of the distillation tower 3 is 0.76MPa, the bottom temperature is 185°C, and the top temperature is 105°C. The condensed oil and the product gasoline blending component oil are separated by distillation.

[0040] It has been determined that the octane number of light diesel after hydrogenation modification and hydrofining treatment is 81.5, an increase of 1.0 octane unit, and the octane number of the product gasoline blending component oil is 86.5.

[0041] Comparative Example: The difference from Example 1 is that no light diesel is added to the raw materials, that is, the feed rate of etherified heavy gasoline is 40 t / h, the feed rate of light diesel is 0 t / h, and the circulating hydrogen amount in hydrogen is 20000 Nm 3 / h, the amount of new hydrogen is 1500Nm 3 / h. The specific steps are as follows: In the first step, the etherified heavy gasoline and hydrogen are mixed and then enter the hydro-reforming unit 1 for hydro-reforming reaction. The inlet temperature of the hydro-reforming unit 1 is 384°C, the bed temperature drop is -13°C, the reaction pressure is 2.5MPa (G), the volume hydrogen-to-oil ratio is 245, and the catalyst volume space velocity is 1.0h -1 , the hydro-reforming catalyst is Fo-35m catalyst, and a hydro-reforming reaction product is obtained; In the second step, the hydrorefining reaction product enters the hydrorefining unit 2 for hydrorefining reaction. The inlet temperature of the hydrorefining unit 2 is 265°C, the outlet temperature is 320°C, the reaction pressure is 2.5MPa (G), the volume hydrogen-to-oil ratio is 245, and the catalyst volume space velocity is 1.0h -1 , the hydrotreating catalyst is PHG-111 catalyst, and a hydrotreating reaction product is obtained; In the third step, the hydrotreating reaction product enters the distillation unit. The top pressure of the distillation tower 3 is 0.76MPa, the bottom temperature is 185°C, and the top temperature is 105°C. The condensed oil and gasoline products are separated by distillation.

[0042] Light diesel (octane number was measured to be 80.5) was added to the gasoline line product at an addition rate of 8 t / h, and the octane number of the obtained mixed gasoline blending component was 86.3. Compared with the results of Example 1, the octane number of the mixed gasoline blending component of this comparative example was 0.3 units lower than the octane number of the gasoline blending component oil of Example 1. This shows that the light diesel enters the hydro-reforming unit 1, undergoes hydrocracking, isomerization, cyclization and other reactions, shortens the molecular carbon chain, and improves the octane number of the light diesel.

[0043] In summary, the present invention uses light diesel as a raw material for gasoline hydrogenation and reforming, thereby increasing the output of basic gasoline components, enriching the processing routes of light diesel, solving the problem of a large amount of high-flash point and high-cetane number high-quality diesel occupied by light diesel when it is transferred into the diesel pool, and improving the flexibility of the refinery's production route when responding to market fluctuations.

[0044] The above technical features constitute the embodiments of the present invention, which have strong adaptability and implementation effect. Non-essential technical features can be added or reduced according to actual needs to meet the requirements of different situations.

Claims

1. A method for producing gasoline blending oil using light diesel as raw material, characterized in that Follow these steps: In the first step, the raw materials of light diesel, etherified heavy gasoline and hydrogen are mixed and then enter the hydro-reforming unit, and the hydro-reforming reaction is carried out under the action of the hydro-reforming catalyst to obtain the hydro-reforming reaction product; In the second step, the hydro-refining reaction product enters the hydro-refining unit, and undergoes a hydro-refining reaction under the action of a hydro-refining catalyst to obtain a hydro-refining reaction product; In the third step, the hydrotreating reaction product enters the distillation unit for distillation separation to obtain condensate oil and product gasoline blending component oil.

2. The method for producing gasoline blending oil using light diesel as raw material according to claim 1, characterized in that In the first step, the feed ratio of light diesel and etherified heavy gasoline is 4 to 9:40, and the circulating hydrogen amount in hydrogen is 19500Nm 3 / h to 20500Nm 3 / h, the amount of new hydrogen is 1400Nm 3 / h to 1600Nm 3 / h.

3. The method for producing gasoline blending oil using light diesel as raw material according to claim 1 or 2, characterized in that In the first step, the light diesel in the raw material is a by-product of a hydrocarbon recombination unit or a diesel hydrogenation unit. The distillation range of the light diesel is 135°C to 235°C, the flash point is less than 62°C, and the density is 803Kg / m 3 Up to 809Kg / m 3 ; or / and, the etherified heavy gasoline is the bottom product of the raw material cutting tower of the gasoline etherification unit, and the distillation range is 80°C to 196°C.

4. The method for producing gasoline blending oil using light diesel as raw material according to any one of claims 1 to 3, characterized in that In the first step, the hydrogenation catalyst is a Ni / Zn molecular sieve structure, and the catalyst model is Fo-35m.

5. The method for producing gasoline blending oil using light diesel as raw material according to any one of claims 1 to 4, characterized in that In the first step, the process conditions of hydrogenation reforming are: reaction pressure 2.4MPa to 2.55MPa, volume hydrogen-to-oil ratio 240 to 250, and reaction inlet temperature 380°C to 390°C.

6. The method for producing gasoline blending oil using light diesel as raw material according to any one of claims 1 to 5, characterized in that In the second step, the hydrotreating catalyst is a Co / Mo-alumina supported structure, and the catalyst model is PHG-111.

7. The method for producing gasoline blending oil using light diesel as raw material according to any one of claims 1 to 6, characterized in that In the second step, the process conditions of hydrotreating are reaction pressure of 2.0 MPa to 2.4 MPa, reaction inlet temperature of 245°C to 280°C, and reaction outlet temperature of 285°C to 340°C.

8. The method for producing gasoline blending oil using light diesel as raw material according to any one of claims 1 to 7, characterized in that The process conditions of the distillation unit are as follows: the bottom temperature of the distillation tower is 180°C to 220°C, the top temperature is 85°C to 140°C, the top operating pressure is 0.7MPa to 1.0MPa, the separated product condensate oil is obtained at the top of the distillation tower, and the product gasoline blending component oil is obtained at the bottom of the tower.

9. A device for implementing the method for producing gasoline blending oil using light diesel as raw material as claimed in any one of claims 1 to 8, characterized in that It includes a hydro-modification unit, a hydro-refining unit and a distillation unit. The distillation unit includes a distillation tower, an air cooler, a circulating water cooler and a tower top reflux tank. The feed end of the hydro-modification unit is fixedly connected with a raw material pipeline, the feed end of the raw material pipeline is fixedly connected with a light diesel pipeline, a hydrogen pipeline and an etherified heavy gasoline pipeline, a de-hydro-refining pipeline is fixedly connected between the discharge end of the hydro-modification unit and the feed end of the hydro-refining unit, a de-distillation pipeline is fixedly connected between the discharge end of the hydro-refining unit and the first feed end of the distillation tower, a first cooling pipeline is fixedly connected between the top discharge end of the distillation tower and the feed end of the air cooler, a second cooling pipeline is fixedly connected between the discharge end of the air cooler and the feed end of the circulating water cooler, a third cooling pipeline is fixedly connected between the discharge end of the circulating water cooler and the feed end of the tower top reflux tank, a condensed oil pipeline is fixedly connected to the discharge end of the tower top reflux tank, and a product gasoline blending component oil pipeline is fixedly connected to the bottom discharge end of the distillation tower.

10. The device according to claim 9, characterized in that A reflux pipeline is fixedly connected between the condensed oil pipeline and the second feed end of the distillation tower.

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