阅读说明：本技术 一种加工重油的方法 (Method for processing heavy oil ) 是由 廖志新 佘玉成 王翠红 王红 申海平 于 2019-01-11 设计创作，主要内容包括：本发明涉及烃油加工领域,公开了一种加工重油的方法,包括：A：将重油原料引入至浆态床加氢单元中进行加氢处理,得到含有催化剂的尾油混合物和轻质产品I；B：将溶剂和所述尾油混合物引入至溶剂脱沥青单元中进行溶剂脱沥青处理,得到脱沥青油混合物和含有催化剂的脱油沥青混合物；C：将所述脱沥青油混合物引入至催化裂化单元中进行催化裂化处理,得到催化裂化油浆和轻质产品II；D：将至少部分所述脱油沥青混合物循环回所述浆态床加氢单元中进行加氢处理。本发明的方法能够提高高附加值产品的收率和重油加工的整体收益。(The invention relates to the field of hydrocarbon oil processing, and discloses a method for processing heavy oil, which comprises the following steps: a: introducing a heavy oil raw material into a slurry bed hydrogenation unit for hydrogenation treatment to obtain a tail oil mixture containing a catalyst and a light product I; b: introducing a solvent and the tail oil mixture into a solvent deasphalting unit for solvent deasphalting treatment to obtain a deasphalted oil mixture and a deoiled asphalt mixture containing a catalyst; c: introducing the deasphalted oil mixture into a catalytic cracking unit for catalytic cracking treatment to obtain catalytic cracking slurry oil and a light product II; d: recycling at least a portion of the deoiled asphalt mixture to the slurry bed hydrogenation unit for hydroprocessing. The method of the invention can improve the yield of high value-added products and the overall benefit of heavy oil processing.)

1. A method of processing heavy oil, the method comprising:

a: introducing a heavy oil raw material into a slurry bed hydrogenation unit for hydrogenation treatment to obtain a tail oil mixture containing a catalyst and a light product I;

b: introducing a solvent and the tail oil mixture into a solvent deasphalting unit for solvent deasphalting treatment to obtain a deasphalted oil mixture and a deoiled asphalt mixture containing a catalyst;

c: introducing the deasphalted oil mixture into a catalytic cracking unit for catalytic cracking treatment to obtain catalytic cracking slurry oil and a light product II;

d: recycling at least a portion of the deoiled asphalt mixture to the slurry bed hydrogenation unit for hydroprocessing.

2. The process according to claim 1, wherein in step B, the solvent deasphalting treatment is carried out in an extraction column of the solvent deasphalting unit and the operating conditions in the extraction column comprise: the temperature is 60-280 ℃, the pressure is 1.0-6.0MPa, and the weight ratio of the solvent/tail oil mixture is (1.0-8.0): 1.

3. the process of claim 1 or 2, wherein the solvent in the solvent deasphalting treatment is selected from at least one of alkanes of C3-C5 or alkenes of C3-C5;

preferably, the solvent in the solvent deasphalting treatment is a solvent separated from the liquefied gas produced in the catalytic cracking unit and/or the slurry bed hydrogenation unit.

4. The process of any one of claims 1 to 3, wherein in step A, the catalyst has an average particle size of 0.01 to 200 microns.

5. The method of any of claims 1-4, wherein the method further comprises: subjecting the deasphalted oil mixture obtained in step B to a solvent recovery treatment before introducing the deasphalted oil mixture into a catalytic cracking unit for catalytic cracking treatment.

6. The process according to any one of claims 1-4, wherein the deoiled asphalt mixture recycled to the slurry bed hydrogenation unit represents 90-98 wt% of the total deoiled asphalt mixture obtained from step B.

7. The method of any of claims 1-6, wherein the method further comprises: and B, before the deoiled asphalt mixture is recycled to the slurry bed hydrogenation unit for hydrogenation treatment, carrying out solvent recovery treatment on the deoiled asphalt mixture obtained in the step B.

8. The method of any of claims 1-7, wherein the method further comprises: before the deoiled asphalt mixture is recycled to the slurry bed hydrogenation unit for hydrotreating, the deoiled asphalt mixture is mixed with a catalytic cracking product to obtain mixed oil, and then the mixed oil is introduced into the slurry bed hydrogenation unit for hydrotreating.

9. The process of claim 8, wherein the catalytic cracking product is a catalytic cracking slurry oil;

preferably, the catalytic cracking product is the catalytic cracking slurry oil from step C.

10. The process according to claim 8 or 9, wherein the deoiled asphalt mixture and the catalytic cracking product are contained in the mixed oil in a weight ratio of (1-20): 1.

Technical Field

The invention relates to the field of hydrocarbon oil processing, in particular to a method for processing heavy oil.

Background

Crude oil heaviness is becoming more and more severe, the demand for light oil products is increasing, and the processing technology of heavy crude oil and residual oil is receiving more and more attention. The solvent deasphalting technology is one of the important technologies for the heavy oil lightening, and the combined process is an attractive development direction for the maximum processing and utilization of the heavy oil.

Solvent deasphalting is a physical process of liquid-liquid extraction, which separates the components of residual oil according to the different solubilities of the solvent. Solvent deasphalting can concentrate asphaltene, metals and the like in residual oil in asphalt to obtain the deasphalted asphalt and deasphalted oil with low impurity content and good cracking performance. The yield of the deasphalted oil and the yield of the deoiled hard asphalt in the solvent deasphalting process are mutually restricted, namely, the deasphalted oil with high yield is obtained while the lower-yield and worse-quality deasphalted asphalt is inevitably remained. The deoiled asphalt obtained from C4 hydrocarbon is inferior and difficult to be utilized, and the development of solvent deasphalting technology is restricted.

A slurry bed reactor is a reactor in which a gas is bubbled through a liquid (slurry) layer in which solid fine particles are suspended to effect a gas-liquid-solid phase reaction process. The slurry bed hydrogenation process has both thermal reaction and moderate hydrogenation of products, and adopts a dispersed catalyst with low cost to pass through a reactor once, which is also called a suspension bed hydrogenation process. The heavy oil slurry bed hydrogenation process has strong raw material adaptability and is suitable for processing inferior heavy oil, but has the problem that catalyst fine powder is difficult to separate. Especially, when the catalyst is a relatively expensive organic compound containing metals such as molybdenum and cobalt, the separation and recycling of the catalyst has become a problem which is difficult to avoid.

CN101892074A introduces a combined process for processing heavy oil by efficiently utilizing deasphalted oil, which combines five processing processes of a solvent deasphalting process, a deasphalted oil solvent extraction process, a catalytic cracking slurry topping process and asphalt blending. The process takes vacuum residue oil as a raw material of a solvent deasphalting process, and deasphalted oil and deoiled asphalt are obtained by separation; separating the deasphalted oil into raffinate oil and extract oil by a solvent extraction process; mixing raffinate oil and other catalytic cracking raw materials, and treating by a catalytic cracking process to obtain a corresponding light product and catalytic cracking slurry oil; carrying out catalytic cracking slurry topping technology treatment on the catalytic cracking slurry to obtain light slurry and heavy slurry; and finally, blending the deoiled asphalt, the extract oil and the topping heavy oil slurry according to a proportion to obtain a road asphalt product. The process has certain requirements on raw materials, and in order to meet the limitation of road asphalt on the wax content, the requirements that the wax content is not more than 3.0 weight percent are provided for deoiled asphalt, extract oil and heavy end-pull oil slurry.

CN104560183A introduces a heavy oil hydro-conversion method, which utilizes a solvent deasphalting process to separate unconverted oil of a heavy oil hydro-thermal cracking reaction to obtain deasphalted oil and deoiled asphalt containing catalyst fine powder, wherein the deoiled asphalt returns to a heavy oil hydro-thermal cracking reactor for continuous reaction, so that the activity of the catalyst can be maintained, the addition of a fresh catalyst is reduced, and the cost is reduced. The method can obviously improve the conversion rate of heavy oil and the yield of light oil. However, the method is easy to block pipelines when the de-asphalted asphalt is conveyed, and the improvement of the yield of the de-asphalted oil in the solvent de-asphalting process is limited.

Disclosure of Invention

The object of the present invention is to overcome the aforementioned drawbacks of the prior art and to provide a new process for processing heavy oil which is capable of increasing the yield of high value-added products and the overall yield of heavy oil processing.

In order to achieve the above object, the present invention provides a method for processing heavy oil, comprising:

a: introducing a heavy oil raw material into a slurry bed hydrogenation unit for hydrogenation treatment to obtain a tail oil mixture containing a catalyst and a light product I;

b: introducing a solvent and the tail oil mixture into a solvent deasphalting unit for solvent deasphalting treatment to obtain a deasphalted oil mixture and a deoiled asphalt mixture containing a catalyst;

c: introducing the deasphalted oil mixture into a catalytic cracking unit for catalytic cracking treatment to obtain catalytic cracking slurry oil and a light product II;

d: recycling at least a portion of the deoiled asphalt mixture to the slurry bed hydrogenation unit for hydroprocessing.

The method for processing the heavy oil can obtain the deasphalted oil with low metal content, low carbon residue value and relatively high additional value and the deasphalted asphalt containing the catalyst fine powder and having high metal content, high carbon residue value and relatively enriched colloid and asphaltene. Because the raw material tail oil mixture of the solvent deasphalting unit is subjected to hydrogenation treatment in the slurry bed hydrogenation unit, the carbon residue value and the impurity content of the deasphalting oil are obviously reduced. After the catalytic cracking slurry oil generated by the catalytic cracking process is mixed with the deoiled asphalt containing the catalyst fine powder, the softening point and viscosity of the deoiled asphalt can be reduced, the conveying performance is improved, and the utilization range of the catalytic cracking slurry oil is enlarged.

In addition, the conveying performance of the deasphalted asphalt is improved, so that the yield of the deasphalted oil in the solvent deasphalting process can be relatively improved, and more deasphalted oil can enter a catalytic cracking device to produce high value-added products.

And the deoiled asphalt solution containing the catalyst fine powder produced in the solvent deasphalting process can be directly mixed with catalytic cracking slurry oil without a solvent recovery process such as stripping and/or flash evaporation and then is conveyed to a slurry bed hydrogenation process device as a raw material, and the solvent can be supplemented by C4-C5 alkane and the like separated from catalytic cracking dry gas or dry gas produced in the slurry bed hydrogenation process, so that the investment of equipment such as a deoiled asphalt stripping tower and the like is reduced, and the solvent recovery energy consumption is also reduced.

Drawings

FIG. 1 is a schematic flow diagram of a heavy oil processing method according to a preferred embodiment of the present invention.

Description of the reference numerals

1. 2, 3, 6, 7, 8, 10, 11, 13, 14, 16 and 17 are all pipelines

4. 12 are all mixers

5. Solvent deasphalting unit

9. Catalytic cracking unit

15. Slurry bed hydrogenation unit

Detailed Description

The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.

As previously mentioned, the present invention provides a process for processing heavy oil, the process comprising:

a: introducing a heavy oil raw material into a slurry bed hydrogenation unit for hydrogenation treatment to obtain a tail oil mixture containing a catalyst and a light product I;

b: introducing a solvent and the tail oil mixture into a solvent deasphalting unit for solvent deasphalting treatment to obtain a deasphalted oil mixture and a deoiled asphalt mixture containing a catalyst;

c: introducing the deasphalted oil mixture into a catalytic cracking unit for catalytic cracking treatment to obtain catalytic cracking slurry oil and a light product II;

d: recycling at least a portion of the deoiled asphalt mixture to the slurry bed hydrogenation unit for hydroprocessing.

Since the tail oil mixture in step B, which is involved in the solvent deasphalting process, contains a catalyst, it is preferred that the solvent deasphalting unit contain a high flux of internals to prevent plugging and to ensure a continuous and stable performance of the process of the invention.

In the present invention, the tail oil mixture may be a mixture containing a catalyst and a residual oil, for example, the tail oil mixture may be a fraction having an initial boiling point of > 524 ℃.

In the invention, the catalytic cracking slurry oil can be a fraction with a distillation range of 343-593 ℃.

Preferably, in step B, the solvent deasphalting treatment is carried out in an extraction column of the solvent deasphalting unit, and the operating conditions in the extraction column include: the temperature is 60-280 ℃, the pressure is 1.0-6.0MPa, and the weight ratio of the solvent/tail oil mixture is (1.0-8.0): 1.

preferably, the solvent in the solvent deasphalting treatment is selected from at least one of C3-C5 alkane or C3-C5 alkene.

According to a preferred embodiment, the solvent in the solvent deasphalting treatment is a solvent separated from the liquefied gas produced in the catalytic cracking unit and/or the slurry bed hydrogenation unit.

Preferably, in step A, the catalyst has an average particle size of from 0.01 to 200 microns, more preferably from 0.2 to 50 microns. That is, the catalyst participating in the hydroprocessing in the slurry bed hydrogenation unit is a fine powder-based catalyst.

In the present invention, in step a, the catalyst participating in the hydrotreatment in the slurry bed hydrogenation unit may be a conventional hydrocracking catalyst. The specific composition of the catalyst participating in the hydrotreatment in the slurry bed hydrogenation unit is not particularly limited in the present invention, and may be various catalysts for hydrocracking conventionally used in the art, for example, a catalyst of the composition disclosed in CN 106669787A.

In the present invention, in step C, the catalyst participating in the catalytic cracking process in the catalytic cracking unit may be a conventional MIP process technology catalyst. The specific composition of the catalyst involved in the catalytic cracking treatment in the catalytic cracking unit is not particularly limited in the present invention, and various catalysts for catalytic cracking conventionally used in the art may be used, for example, a catalyst having the composition disclosed in CN 1217231A.

In the present invention, the light product I may contain, for example, gas, gasoline, diesel oil, wax oil, and the like.

In the present invention, the light product II may contain, for example, dry gas, liquefied gas, gasoline, diesel oil, or the like.

The process of the present invention does not particularly limit the operating conditions in the slurry bed hydrogenation unit and the catalytic cracking unit, and those skilled in the art can perform the process using the operating conditions conventionally used in the art, and the operating conditions in the slurry bed hydrogenation unit and the catalytic cracking unit are exemplified in the examples of the present invention, and those skilled in the art should not be construed as limiting the process of the present invention.

According to a preferred embodiment, the method of the invention further comprises: subjecting the deasphalted oil mixture obtained in step B to a solvent recovery treatment before introducing the deasphalted oil mixture into a catalytic cracking unit for catalytic cracking treatment.

Preferably, the deoiled asphalt mixture recycled to the slurry bed hydrogenation unit accounts for 90-98 wt% of the total deoiled asphalt mixture obtained from step B, more preferably the deoiled asphalt mixture recycled to the slurry bed hydrogenation unit accounts for 95-98 wt% of the total deoiled asphalt mixture obtained from step B.

According to a preferred embodiment, the method of the invention further comprises: and B, before the deoiled asphalt mixture is recycled to the slurry bed hydrogenation unit for hydrogenation treatment, carrying out solvent recovery treatment on the deoiled asphalt mixture obtained in the step B.

In the present invention, if the deasphalted oil mixture obtained in step B is subjected to a solvent recovery treatment before the deasphalted oil mixture is introduced into a catalytic cracking unit to be subjected to a catalytic cracking treatment, the weight ratio of the deasphalted oil mixture to be recycled to the slurry bed hydrogenation unit is calculated as a form before the solvent recovery treatment is carried out.

In order to further increase the yield of high value added products, according to another preferred embodiment, the method of the invention further comprises: before the deoiled asphalt mixture is recycled to the slurry bed hydrogenation unit for hydrotreating, the deoiled asphalt mixture is mixed with a catalytic cracking product to obtain mixed oil, and then the mixed oil is introduced into the slurry bed hydrogenation unit for hydrotreating.

Preferably, the catalytic cracking product is catalytic cracking slurry oil.

Particularly preferably, the catalytic cracking product is the catalytic cracking slurry oil from step C.

Preferably, in the mixed oil, the content weight ratio of the deoiled asphalt mixture and the catalytic cracking product is (1-20): 1, more preferably, the weight ratio of the contents of the deoiled asphalt mixture and the catalytic cracking product is (2-5): 1.

the following provides a preferred embodiment of the process for heavy oil processing of the present invention:

a: introducing a heavy oil raw material into a slurry bed hydrogenation unit for hydrogenation treatment to obtain a tail oil mixture containing a catalyst and a light product I;

b: introducing a solvent and the tail oil mixture into an extraction tower of a solvent deasphalting unit for solvent deasphalting treatment to obtain a deasphalted oil mixture and a catalyst-containing deasphalted oil mixture;

c: recovering the deasphalted oil mixture by using a solvent, and introducing the deasphalted oil mixture into a catalytic cracking unit for catalytic cracking treatment to obtain catalytic cracking slurry oil and a light product II;

d: and (3) after at least part of the deoiled asphalt mixture is subjected to or not subjected to solvent recovery treatment, partially throwing outwards, mixing the rest part with the catalytic cracking slurry oil, and then circulating the mixture back to the slurry bed hydrogenation unit for hydrogenation treatment.

A preferred embodiment of the process for heavy oil processing of the present invention is provided below in conjunction with fig. 1:

the tail oil mixture containing catalyst fine powder produced by the slurry bed hydrogenation unit 15 is mixed with a part of solvent in a mixer 4 through a pipeline 1 after passing through a pipeline 3 (wherein the mass ratio of the solvent to the tail oil mixture is (0.3-1):1, preferably (0.4-0.6):1), enters a solvent deasphalting unit 5, a part of the solvent enters a solvent deasphalting unit 5 from the bottom of an extraction tower through a pipeline 2 (the weight ratio of the part of the solvent to the tail oil mixture is (2-7):1, preferably (2-3):1), deasphalted oil and a deasphalted asphalt mixture containing catalyst fine powder are obtained, a part of the deasphalted asphalt mixture is thrown out through a pipeline 8, and the mass percent of the thrown-out amount is 2-10%, preferably 2-5%. The deasphalted oil is introduced into a catalytic cracking unit 9 through a pipeline 6, and a catalytic cracking reaction is carried out under conventional process conditions to obtain a corresponding light product II and catalytic cracking slurry oil, and the light product II is led out through a pipeline 10. The catalytically cracked slurry oil produced by catalytic cracking unit 9 is introduced via line 11 into mixer 12 for mixing with the partially de-oiled asphalt mixture introduced via line 7; and/or other catalytically cracked oil slurry from outside the system is introduced via line 17 into mixer 12 to be mixed with the partially de-oiled asphalt mixture introduced via line 7 to obtain a mixed oil which is hydrotreated in slurry bed hydrogenation unit 15 along with the heavy oil feedstock containing fresh catalyst fines introduced via line 13 and hydrogen withdrawn via line 14. The corresponding light product I obtained after treatment in the slurry bed hydrogenation unit 15 is withdrawn via line 16 and the obtained tail oil mixture containing catalyst fines is introduced via line 3 into the solvent deasphalting unit 5.

The equipment involved in the catalytic cracking unit and the slurry bed hydrogenation unit are conventional equipment; because the raw materials treated contain solid powder, the raw material conveying system of the solvent deasphalting unit preferably adopts anti-blocking measures, and the extraction tower preferably adopts an inner member with high passing performance so as to ensure the continuous and stable operation of the device.

The invention is further illustrated by the following preferred exemplary examples. The aim has been to better illustrate the invention and the scope of protection is not limited by the examples given.