Method and device for producing gasoline blending oil from light diesel oil

Abstract

The present application relates to gasoline processing technical field, it is a kind of method and device for producing gasoline blending oil with light diesel oil as raw material, the former is carried out according to the following steps: first, raw material light diesel oil, etherification heavy gasoline and hydrogen are mixed and then enter hydrogen modification unit, hydrogen modification reaction is carried out under the action of hydrogen modification catalyst, and hydrogen modification reaction product is obtained;Second step, hydrogen modification reaction product enters hydrogen refining unit, hydrogen refining reaction is carried out under the action of hydrogen refining catalyst, and hydrogen refining reaction product is obtained;Third step, hydrogen refining reaction product enters rectification unit, and condensation oil and product gasoline blending component oil are obtained by rectification separation.The light diesel oil, hydrogen and etherification heavy gasoline are mixed to carry out hydrogen modification and hydrogen refining treatment, and product gasoline blending component oil is obtained, the octane number of light diesel oil is effectively increased, the yield of base gasoline component is improved, has higher economic benefit, and the processing route of light diesel oil is widened.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of gasoline processing, and is a method and device for producing gasoline blending oil from light diesel oil as raw material. BACKGROUND

[0002] The light diesel oil, which is a byproduct of a hydrocarbon reforming device or a diesel hydrogenation device (under a naphtha processing scheme), has a distillation range of 135 DEG C to 235 DEG C. Compared with refined diesel oil of the diesel hydrogenation device, the light diesel oil has a lower flash point and a lower cetane number, and is a component between gasoline and diesel oil in terms of distillation range. Compared with catalytic cracking heavy gasoline, the light diesel oil has a higher aromatic content and a lower olefin content, and the olefin molecules are long-chain molecules, and the octane number 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 about 9 to 10 units higher.

[0003] At present, the light diesel oil is processed into a diesel blending pool to participate in diesel blending. However, because the light diesel oil has a low flash point and a low cetane number, a large amount of high-flash-point high-cetane diesel oil is needed for blending, which wastes a large amount of high-quality diesel oil, and the processing route of the light diesel oil is relatively single.

[0004] To solve this problem, some refineries change the light diesel oil back to the diesel hydrogenation device as raw material, and the light diesel oil is subjected to a hydrogenation refining reaction in a reaction stage and then is subjected to fractionation in a fractionating tower to cut the light diesel oil into naphtha and diesel oil components, so as to change the flash point of the diesel oil. The light diesel oil is reprocessed, the processing cost is increased, and the diesel oil yield after processing is reduced to about 50%, and 50% is converted into naphtha components. The entire processing process does not increase high-value-added products, and the quality is not improved. SUMMARY

[0005] The present application provides a method and device for producing gasoline blending oil from light diesel oil as raw material, which overcomes the above-mentioned deficiencies of the prior art and effectively solves the problems of a single processing route and high processing cost of the light diesel oil.

[0006] One of the technical solutions of the present application is achieved by the following measures: a method for producing gasoline blending oil from light diesel oil as raw material, which is performed according to the following steps:

[0007] In a first step, the raw material light diesel oil, etherified heavy gasoline and hydrogen are mixed and then are introduced into a hydro-upgrading unit to perform a hydro-upgrading reaction under the action of a hydro-upgrading catalyst, so as to obtain a hydro-upgrading reaction product;

[0008] In a second step, the hydro-upgrading reaction product is introduced into a hydrofining unit to perform a hydrofining reaction under the action of a hydrofining catalyst, so as to obtain a hydrofining reaction product;

[0009] In the third step, the hydrogenation reaction product is introduced into a rectification unit to separate condensed oil and product gasoline blending component oil.

[0010] The following is a further optimization or / and improvement of one of the above technical solutions:

[0011] In the first step, the ratio of the feed amount of light diesel oil to etherified heavy gasoline is 4 to 9:40, the amount of recycled hydrogen in hydrogen is 19500 Nm 3 / h to 20500 Nm 3 / h, and the amount of new hydrogen is 1400 Nm 3 / h to 1600 Nm 3 / h.

[0012] In the first step, the light diesel oil in the raw material is a byproduct of a hydrocarbon reforming device or a diesel hydrogenation device (under the naphtha processing scheme), the distillation range of the light diesel oil is 135℃ to 235℃, the flash point is less than 62℃, and the density is 803 Kg / m 3 to 809 Kg / m 3 .

[0013] In the first step, the etherified heavy gasoline in the raw material is the bottom product of the gasoline etherification device cutting tower, the distillation range is 80℃ to 196℃, and it belongs to the heavy component of catalytic cracking gasoline.

[0014] In the first step, the hydrogenation modification catalyst is a Ni / Zn molecular sieve structure, and the catalyst type is Fo-35m. The Fo-35m catalyst used in the present application is developed and produced by Fushun Petrochemical Company of China Petroleum.

[0015] In the first step, the process conditions for hydrogenation modification are: reaction pressure 2.4MPa to 2.55MPa (G), volume hydrogen oil ratio 240 to 250, reaction inlet temperature 380℃ to 390℃. Preferably, the reaction pressure of the hydrogenation modification unit is 2.5MPa (G), the reaction inlet temperature is 384℃, and the volume hydrogen oil ratio is 245.

[0016] In the second step, the hydrogenation refining catalyst is a Co / Mo-alumina supported structure, and the catalyst type is PHG-111.

[0017] In the second step, the process conditions for hydrogenation refining are: reaction pressure 2.0MPa to 2.4MPa (G), reaction inlet temperature 245℃ to 280℃, and reaction outlet temperature 285℃ to 340℃. Preferably, the reaction pressure of the hydrogenation refining unit is 2.1MPa (G), the reaction inlet temperature is 262℃, and the reaction outlet temperature is 320℃.

[0018] The process conditions of the rectification unit are as follows: the bottom temperature of the rectification tower is 180-220 DEG C, the top temperature is 85-140 DEG C, the operating pressure at the top is 0.7-1.0 MPa, the separation product condensed oil is obtained at the top of the rectification tower, and the product gasoline blending component oil is obtained at the bottom.

[0019] The second technical solution of the present application is realized by the following measures: a device for implementing a method for producing gasoline blending oil by using light diesel oil as raw material, comprising a hydro-upgrading unit, a hydrofining unit and a rectification unit, the rectification unit comprises a rectification tower, an air cooler, a circulating water cooler and a tower top reflux tank, the hydro-upgrading unit is fixedly connected with a raw material pipeline at the feeding end, the raw material pipeline is fixedly connected with a light diesel oil pipeline, a hydrogen pipeline and an etherified heavy gasoline pipeline at the feeding end, the hydro-upgrading unit is fixedly connected with a hydrofining pipeline between the discharging end and the feeding end of the hydrofining unit, the hydrofining unit is fixedly connected with a rectification pipeline between the discharging end and the first feeding end of the rectification tower, the rectification tower is fixedly connected with a first cooling pipeline between the discharging end at the top and the feeding end of the air cooler, the air cooler is fixedly connected with a second cooling pipeline between the discharging end and the feeding end of the circulating water cooler, the circulating water cooler is fixedly connected with a third cooling pipeline between the discharging end and the feeding end of the tower top reflux tank, the tower top reflux tank is fixedly connected with a condensed oil pipeline at the discharging end, and the rectification tower is fixedly connected with a product gasoline blending component oil pipeline at the discharging end at the bottom.

[0020] The following is a further optimization or / and improvement of the second technical solution of the present application:

[0021] The condensed oil pipeline is fixedly connected with a reflux pipeline between the second feeding end of the rectification tower.

[0022] The present application provides a method and device for producing gasoline blending oil by using light diesel oil as raw material, which mixes light diesel oil, hydrogen and etherified heavy gasoline, and carries out hydro-upgrading and hydrofining treatment on the obtained mixture, to obtain product gasoline blending component oil, effectively increases the octane number of light diesel oil, improves the yield of base gasoline component, has lower investment and operation cost, has higher economic benefits, and widens the processing route of light diesel oil. BRIEF DESCRIPTION OF DRAWINGS

[0023] ATTACHMENT Figure 1 The process flow diagram of the embodiment 10 of the present application is shown.

[0024] The codes in the drawing are as follows: 1 is a hydro-upgrading unit, 2 is a hydrofining unit, 3 is a rectifying 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 oil pipeline, 9 is a hydrogen pipeline, 10 is an etherified heavy gasoline pipeline, 11 is a dehydrofining pipeline, 12 is a de-rectifying 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

[0025] The present application is not limited by the following examples, and the specific implementation can be determined according to the technical solutions of the present application and the actual situation. In the present application, various chemical reagents and chemical supplies mentioned are commonly known and used in the prior art unless otherwise specified. In the present application, normal temperature and room temperature generally refer to a temperature of 15-25°C, and are generally defined as 25°C.

[0026] In the present application, the equipment and devices used are commonly known and used in the prior art unless otherwise specified.

[0027] The present application is further described below in conjunction with examples:

[0028] Example 1: As shown in the following, the method for producing a gasoline blending oil from light diesel oil as a raw material is carried out in the following steps: Figure 1

[0029] In the first step, the raw material light diesel oil, etherified heavy gasoline, and hydrogen are mixed and then fed into the hydro-upgrading unit 1, where a hydro-upgrading reaction is carried out under the action of a hydro-upgrading catalyst to obtain a hydro-upgrading reaction product.

[0030] In the second step, the hydro-upgrading reaction product is fed into the hydrofining unit 2, where a hydrofining reaction is carried out under the action of a hydrofining catalyst to obtain a hydrofining reaction product.

[0031] In the third step, the hydrofining reaction product is fed into the rectifying unit, and condensed oil and product gasoline blending component oil are obtained by rectification separation.

[0032] Example 2: As an optimization of the above example, in the first step, the ratio of the feed amounts of light diesel oil and etherified heavy gasoline is 4-9:40, the amount of circulating hydrogen in the hydrogen is 19500 Nm 3 / h to 20500 Nm 3 / h, the amount of new hydrogen is 1400 Nm 3 / h to 1600 Nm 3 / h.

[0033] ​Example 3: As an optimization of the above examples, in the first step, the light diesel oil in the raw material is a by-product of a hydrocarbon reforming unit or a diesel hydrogenation unit (under the naphtha processing scheme), the distillation range of the light diesel oil is 135°C to 235°C, the flash point is less than 62°C, and the density is 803 Kg / m 3 to 809 Kg / m 3 The main properties of the light diesel oil used in the present application are shown in Table 1.

[0034] Example 4: As an optimization of the above examples, in the first step, the etherified heavy gasoline in the raw material is the bottom product of the cutting tower of the gasoline etherification unit, the distillation range is 80°C to 196°C, and it belongs to the heavy component of catalytic cracking gasoline.

[0035] Example 5: As an optimization of the above examples, in the first step, the hydro-upgrading catalyst is a Ni / Zn molecular sieve structure, and the catalyst type is Fo-35m. The Fo-35m catalyst used in the present application is developed and produced by Fushun Petrochemical Company of China Petroleum.

[0036] Example 6: As an optimization of the above examples, in the first step, the process conditions of hydro-upgrading are: reaction pressure 2.4 MPa to 2.55 MPa (G), volume hydrogen 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 2.5 MPa (G), the reaction inlet temperature is 384°C, and the volume hydrogen oil ratio is 245.

[0037] Example 7: As an optimization of the above examples, in the second step, the hydrofining catalyst is a Co / Mo-alumina supported structure, and the catalyst type is PHG-111.

[0038] Example 8: As an optimization of the above examples, in the second step, the process conditions of hydrofining are: reaction pressure 2.0 MPa to 2.4 MPa (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 2.1 MPa (G), the reaction inlet temperature is 262°C, and the reaction outlet temperature is 320°C.

[0039] Example 9: As an optimization of the above examples, the process conditions of the rectification unit are: the bottom temperature of the rectification tower 3 is 180°C to 220°C, the top temperature is 85°C to 140°C, the top operating pressure is 0.7 MPa to 1.0 MPa, and the top of the rectification tower 3 obtains the separation product condensed oil and the bottom obtains the separation product product gasoline blending component oil. Preferably, the bottom temperature of the rectification unit is 185°C, the top temperature is 105°C, and the top operating pressure is 0.76 MPa.

[0040] Example 10: As Figure 1As shown, the apparatus for producing gasoline blending oil from light diesel oil includes a hydrotreating unit 1, a hydrorefining unit 2, and a distillation unit. The distillation unit includes a distillation column 3, an air cooler 4, a circulating water cooler 5, and a top reflux tank 6. A feed line 7 is fixedly connected to the feed end of the hydrotreating unit 1. A light diesel oil line 8, a hydrogen line 9, and an etherified heavy gasoline line 10 are fixedly connected to the feed end of the feed line 7. A line 11 is fixedly connected between the discharge end of the hydrotreating unit 1 and the feed end of the hydrorefining unit 2. The hydrorefining unit 2... A distillation pipeline 12 is fixedly connected between the discharge end and the first feed end of the distillation column 3. A first cooling pipeline 13 is fixedly connected between the top discharge end of the distillation column 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 top reflux tank 6. A condensed oil pipeline 17 is fixedly connected to the discharge end of the top reflux tank 6. A product gasoline blending component oil pipeline 18 is fixedly connected to the bottom discharge end of the distillation column 3.

[0041] Example 11: As Figure 1 As shown, as an optimization of the above embodiment, a reflux line 16 is fixedly connected between the condensate oil line 17 and the second feed end of the distillation column 3. Part of the condensate oil is returned to the distillation column 3 through the reflux line 16.

[0042] As required, valves and instruments to ensure the normal operation of the unit producing gasoline blending oil from light diesel oil are fixedly installed on each pipeline. The hydrotreating unit 1, hydrorefining unit 2, and distillation unit all use existing reactors and equipment, and the distillation column 3 is a tray distillation column 3.

[0043] This invention mixes light diesel oil, hydrogen, and etherified heavy gasoline, and then performs hydrotreating and hydrorefining on the resulting mixture to obtain a product gasoline blending component. The light diesel oil, hydrogen, and etherified heavy gasoline mixture enters hydrotreating unit 1 for hydrotreating reactions. These reactions, occurring in a fixed-bed reactor, include hydrocracking, isomerization, aromatization, and cyclization, which shorten the molecular carbon chain and increase the octane number of the light diesel oil. The resulting reaction products enter hydrorefining unit 2 for hydrorefining reactions, including hydrodesulfurization and olefin saturation reactions in a fixed-bed reactor. The reaction products from the hydrorefining reactions are separated by distillation to obtain condensate oil and the product gasoline blending component. The product gasoline blending component enters the base gasoline blending tank, increasing the density of the base gasoline components and reducing the olefin content, thus reducing the need for blending in high-density component oils.

[0044] Example 12: This gasoline blending oil, produced from light diesel oil, is obtained according to the following process steps:

[0045] The octane number of the light diesel oil in the raw material is 80.5, the etherification heavy gasoline feed amount is 40 t / h, the light diesel oil feed is 8 t / h, the amount of recycled hydrogen in the hydrogen is 20,000 Nm 3 / h, and the amount of new hydrogen is 1,500 Nm 3 / h.

[0046] In the first step, the light diesel oil, the etherification heavy gasoline, and the hydrogen are mixed and then enter a hydro-upgrading unit 1 to perform a hydro-upgrading reaction. The inlet temperature of the hydro-upgrading unit 1 is 384°C, the bed temperature drop is -13°C, the reaction pressure is 2.5 MPa (G), the volume hydrogen to oil ratio is 245, and the hydro-upgrading catalyst is Fo-35m catalyst. The hydro-upgrading reaction product is obtained.

[0047] In the second step, the hydro-upgrading reaction product enters a hydrofining unit 2 to perform a hydrofining reaction. The inlet temperature of the hydrofining unit 2 is 265°C, the outlet temperature is 320°C, the reaction pressure is 2.1 MPa (G), the hydrofining catalyst is PHG-111 catalyst, and the hydrofining reaction product is obtained.

[0048] In the third step, the hydrofining reaction product enters a rectification unit. The rectification column 3 has a top pressure of 0.76 MPa, a bottom temperature of 185°C, and a top temperature of 105°C. The rectification separation obtains condensed oil and product gasoline blending component oil.

[0049] It is determined that the octane number of the light diesel oil after the hydro-upgrading and the hydrofining treatment is 82.0, which increases by 1.5 units of octane number. The octane number of the product gasoline blending component oil is 86.6.

[0050] In example 13, the gasoline blending oil produced from the light diesel oil as the raw material is produced according to the following process steps:

[0051] The octane number of the light diesel oil in the raw material is 80.5, the etherification heavy gasoline feed amount is 40 t / h, the light diesel oil feed is 5 t / h, the amount of recycled hydrogen in the hydrogen is 20,000 Nm 3 / h, and the amount of new hydrogen is 1,500 Nm 3 / h.

[0052] In the first step, the light diesel oil, the etherification heavy gasoline, and the hydrogen are mixed and then enter a hydro-upgrading unit 1 to perform a hydro-upgrading reaction. The inlet temperature of the hydro-upgrading unit 1 is 384°C, the bed temperature drop is -13°C, the reaction pressure is 2.5 MPa (G), the volume hydrogen to oil ratio is 245, and the hydro-upgrading catalyst is Fo-35m catalyst. The hydro-upgrading reaction product is obtained. -1

[0053] ​The hydrogenation upgrading reaction product enters a hydrogenation refining unit 2 to perform a hydrogenation refining reaction, the inlet temperature of the hydrogenation refining unit 2 is 265°C, the outlet temperature is 320°C, the reaction pressure is 2.1 MPa (G), the hydrogenation refining catalyst is PHG-111 catalyst, and a hydrogenation refining reaction product is obtained;

[0054] The hydrogenation refining reaction product enters a rectification unit, the top pressure of the rectification column 3 is 0.76 MPa, the bottom temperature is 185°C, and the top temperature is 105°C, and condensed oil and product gasoline blending component oil are obtained through rectification separation.

[0055] It is determined that the octane number of the light diesel oil after the hydrogenation upgrading and hydrogenation refining treatment is 81.6, which increases by 1.1 octane number units, and the octane number of the product gasoline blending component oil is 86.5.

[0056] Example 14: The gasoline blending oil produced by using light diesel oil as the raw material is produced according to the following process steps:

[0057] The octane number of the light diesel oil in the raw material is 80.5, the etherification heavy gasoline feed amount is 40 t / h, the light diesel oil feed is 10 t / h, the amount of the recycled hydrogen in the hydrogen is 20,000 Nm 3 / h, and the amount of the fresh hydrogen is 1,500 Nm 3 / h;

[0058] The light diesel oil, the etherification heavy gasoline and the hydrogen are mixed and then enter a hydrogenation upgrading unit 1 to perform a hydrogenation upgrading reaction, the inlet temperature of the hydrogenation upgrading unit 1 is 384°C, the bed temperature drop is -13°C, the reaction pressure is 2.5 MPa (G), the volume hydrogen / oil ratio is 245, the catalyst volume space velocity is 1.0 h -1 , the hydrogenation upgrading catalyst is Fo-35m catalyst, and a hydrogenation upgrading reaction product is obtained;

[0059] The hydrogenation upgrading reaction product enters a hydrogenation refining unit 2 to perform a hydrogenation refining reaction, the inlet temperature of the hydrogenation refining unit 2 is 265°C, the outlet temperature is 320°C, the reaction pressure is 2.1 MPa (G), the hydrogenation refining catalyst is PHG-111 catalyst, and a hydrogenation refining reaction product is obtained;

[0060] The hydrogenation refining reaction product enters a rectification unit, the top pressure of the rectification column 3 is 0.76 MPa, the bottom temperature is 185°C, and the top temperature is 105°C, and condensed oil and product gasoline blending component oil are obtained through rectification separation.

[0061] It is determined that the octane number of the light diesel oil after the hydrogenation upgrading and hydrogenation refining treatment is 81.5, which increases by 1.0 octane number units, and the octane number of the product gasoline blending component oil is 86.5.

[0062] Comparative Example: Different from Example 1, no light diesel oil is added in the raw material, that is, the etherification heavy gasoline feed amount is 40 t / h, the light diesel oil feed is 0 t / h, the amount of circulating hydrogen in the hydrogen is 20000 Nm 3 / h, and the amount of new hydrogen is 1500 Nm 3 / h. The specific steps are as follows:

[0063] First step, the etherification heavy gasoline and hydrogen are mixed and then enter the hydro-upgrading unit 1 to perform hydro-upgrading reaction, the inlet temperature of the hydro-upgrading unit 1 is 384℃, the bed temperature drop is-13℃, the reaction pressure is 2.5 MPa (G), the volume hydrogen oil ratio is 245, the catalyst volume space velocity is 1.0 h -1 , the hydro-upgrading catalyst is Fo-35m catalyst, and the hydro-upgrading reaction product is obtained;

[0064] Second step, the hydro-upgrading reaction product enters the hydrofining unit 2 to perform hydrofining reaction, the inlet temperature of the hydrofining unit 2 is 265℃, the outlet temperature is 320℃, the reaction pressure is 2.5 MPa (G), the volume hydrogen oil ratio is 245, the catalyst volume space velocity is 1.0 h -1 , the hydrofining catalyst is PHG-111 catalyst, and the hydrofining reaction product is obtained;

[0065] Third step, the hydrofining reaction product enters the rectification unit, the rectification column 3 top pressure is 0.76 MPa, the column bottom temperature is 185℃, the column top temperature is 105℃, and the rectification separation obtains condensed oil and gasoline linear product.

[0066] The light diesel oil (octane value is measured as 80.5, ) is added into the gasoline linear product according to the addition amount of 8 t / h, and the octane value of the obtained mixed gasoline blending component is 86.3. Compared with the results of Example 1, the octane value of the mixed gasoline blending component of the present comparative example is 0.3 units lower than that of the product gasoline blending component oil of Example 1. Therefore, it is illustrated that the light diesel oil enters the hydro-upgrading unit 1 to perform hydrocracking, isomerization, cyclization and other reactions, shortens the molecular carbon chain, and improves the octane value of the light diesel oil.

[0067] In summary, the present application uses light diesel oil as the raw material of gasoline hydro-upgrading, increases the yield of base gasoline component, enriches the post-processing route of light diesel oil, solves the problem of a large amount of high-flash-point high-cetane-number high-quality diesel oil occupied by the light diesel oil blending into the diesel pool, and improves the flexibility of the production route of the refinery in response to market fluctuations.

[0068] The above technical features constitute an embodiment of the present application, which has strong adaptability and implementation effect. Non-essential technical features can be added or reduced according to actual needs to meet the needs of different situations.

Claims

1. A process for producing gasoline blending stock from light diesel oil, characterized in that The following steps are taken: In the first step, the raw material light diesel oil, etherified heavy gasoline and hydrogen are mixed and then fed into a hydro-upgrading unit to perform a hydro-upgrading reaction under the action of a hydro-upgrading catalyst, to obtain a hydro-upgrading reaction product; In the second step, the hydro-upgrading reaction product is fed into a hydrofining unit to perform a hydrofining reaction under the action of a hydrofining catalyst, to obtain a hydrofining reaction product; In the third step, the hydrofining reaction product is fed into a rectification unit to perform rectification separation to obtain condensed oil and product gasoline blending component oil.

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

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

4. The method for producing gasoline blending stock from light diesel according to claim 1, characterized by In the first step, the hydro-upgrading catalyst is a Ni / Zn molecular sieve structure, and the catalyst model is Fo-35m.

5. The method for producing gasoline blending stock from light diesel according to claim 1 or 4, characterized by In the first step, the process conditions for hydro-upgrading are as follows: reaction pressure 2.4-2.55 MPa, volume hydrogen / oil ratio 240-250, and reaction inlet temperature 380-390℃.

6. The method for producing gasoline blending stock from light diesel according to claim 1, characterized by In the second step, the hydrofining catalyst is a Co / Mo-alumina supported structure, and the catalyst model is PHG-111.

7. The method for producing gasoline blending stock from light diesel according to claim 1 or 6, characterized by In the second step, the process conditions for hydrofining are as follows: reaction pressure 2.0-2.4 MPa, reaction inlet temperature 245-280℃, and reaction outlet temperature 285-340℃.

8. The method for producing gasoline blending stock from light diesel according to claim 1, characterized by The process conditions for the rectification unit are as follows: rectification column bottom temperature 180-220℃, column top temperature 85-140℃, column top operating pressure 0.7-1.0 MPa, and the rectification column top separation product is condensed oil, and the column bottom product is product gasoline blending component oil.

9. An apparatus for carrying out the process according to any one of claims 1 to 8 for producing gasoline blending oil from light diesel oil, characterized in that The rectification unit includes a rectification column, an air cooler, a circulating water cooler and a column top reflux tank, the hydro-upgrading unit feed end is fixedly connected with a raw material pipeline, the raw material pipeline feed end is fixedly connected with a light diesel oil pipeline, a hydrogen pipeline and an etherified heavy gasoline pipeline, the hydro-upgrading unit discharge end is fixedly connected with a hydrofining unit feed end, the hydrofining unit discharge end is fixedly connected with a rectification column first feed end, the rectification column top discharge end is fixedly connected with an air cooler feed end, the air cooler discharge end is fixedly connected with a circulating water cooler feed end, the circulating water cooler discharge end is fixedly connected with a column top reflux tank feed end, the column top reflux tank discharge end is fixedly connected with a condensed oil pipeline, and the rectification column bottom discharge end is fixedly connected with a product gasoline blending component oil pipeline.

10. The apparatus of claim 9, wherein The condensed oil pipeline is fixedly connected with a reflux pipeline and a rectification column second feed end.

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