CN115895722A - System for preparing light aromatic hydrocarbon from heavy oil raw material - Google Patents
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- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 97
- 239000000295 fuel oil Substances 0.000 title claims abstract description 77
- 239000002994 raw material Substances 0.000 title claims abstract description 44
- 239000002283 diesel fuel Substances 0.000 claims abstract description 73
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 69
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 57
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000001257 hydrogen Substances 0.000 claims abstract description 30
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 30
- 238000005336 cracking Methods 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims description 63
- 238000005520 cutting process Methods 0.000 claims description 51
- 239000003921 oil Substances 0.000 claims description 46
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A heavy oil raw material prepares the light aromatic system, it is the reprocessing of the inferior diesel oil in the petroleum refining field, including double lift pipe catalytic cracking unit, main fractionating tower, vice fractionating tower, main cut fractionating tower and vice cut fractionating tower, heavy oil raw material is once catalytic cracking-fractionating in the main fractionating tower-cut in the main cut fractionating tower in the heavy oil lift pipe sequentially and form light fraction and heavy fraction, heavy fraction mix with light fraction and send into the second lift pipe to carry on the second catalytic cracking after the first hydrogenation in the main hydrogenation reactor, the gasohol component that the second cracking produces hydrogenates and enters the cut in the vice cut fractionating tower for the cut in the second hydrogenation, separate light component and heavy fraction, the heavy fraction is sent into the aromatic combination unit finally, separate three kinds of products; in the whole system, secondary catalytic cracking and secondary hydrogenation are required to be carried out on the poor-quality diesel oil, so that the hydrogenation pressure is reduced, the hydrogen consumption is obviously reduced, and the yield of C6-C9 aromatic hydrocarbons in a final product can reach over 50 wt%.
Description
Technical Field
The invention relates to the reprocessing of heavy oil raw materials in the field of petroleum refining, in particular to a system for preparing light aromatic hydrocarbon from heavy oil raw materials.
Background
Heavy oil raw materials refer to oil materials with the distillation range of more than 350 ℃, the existing treatment method generally prepares diesel oil by catalytic cracking in a catalytic cracking device, but the market share of the diesel oil is not changed greatly in recent years, so that the diesel oil is excessive in structure, correspondingly, benzene, toluene and xylene BTX in aromatic hydrocarbon are basic organic chemical raw materials in petrochemical industry, can be used for generating various chemical products such as synthetic rubber, synthetic fiber and synthetic resin, and can also be used for producing various fine chemical products, and the market demand of the BTX is larger and larger.
LCO annual output of low-cetane number inferior diesel oil in China exceeds 10Mt, the LCO annual output is more and more difficult to be used as blending components of automotive diesel oil, the requirements of refineries for blending and producing the automotive diesel oil are difficult to meet even after hydrofining, investment for building a diesel oil hydro-upgrading device is quite large, and the LCO is used for producing light aromatic hydrocarbon and gasoline with high added values, so that the LCO has certain development significance.
At present, the domestic and international research institutions mainly process the poor diesel oil by the processes of hydrocracking, solvent extraction, hydrogenation-reforming, hydrogenation-catalysis and the like to produce aromatic hydrocarbon or gasoline:
CN 103214332 discloses a method for producing light aromatic hydrocarbons and high-quality oil products from catalytic cracking diesel oil, which comprises extracting catalytic cracking diesel oil with a solvent to obtain an extract oil rich in polycyclic aromatic hydrocarbons and a raffinate oil rich in alkanes, and subjecting the extract oil to hydrorefining and hydrocracking under the condition of hydrogenation reaction to produce light aromatic hydrocarbons and high octane gasoline fractions; the method can produce diesel oil with high cetane number and gasoline with high octane number as by-products while obtaining light aromatic hydrocarbon, but the method has low diesel oil utilization rate and low by-product value.
CN 105542849 discloses a method for producing clean diesel oil and light aromatic hydrocarbon from inferior diesel oil, which comprises the steps of removing sulfur nitrogen compounds, olefin and colloid after the inferior diesel oil is subjected to medium-low pressure hydrogenation to obtain hydrorefined diesel oil, removing aromatic hydrocarbon and sulfide from the refined diesel oil through adsorption separation by a simulated moving bed to obtain clean diesel oil and heavy aromatic hydrocarbon, feeding the heavy aromatic hydrocarbon into a light-to-heavy reactor, and carrying out hydrogenation reaction at medium-low pressure to generate BTX light aromatic hydrocarbon, gasoline components and a small amount of light hydrocarbon; the process for producing clean diesel oil and light aromatic hydrocarbon from poor diesel oil provided by the method can be used for treating catalytic cracking diesel oil and coking diesel oil, the components of the generated clean diesel oil and gasoline can meet the national V standard, and the BTX light aromatic hydrocarbon is a byproduct, but the process flow is longer and the conversion depth is lower.
CN106753551A discloses a method for producing gasoline with high octane number by using catalytic cracking diesel oil, the method cuts the catalytic diesel oil into fractions with the temperature of less than 280 ℃ and fractions with the temperature of more than 280 ℃ after hydrofining, raffinate oil obtained by extracting aromatic hydrocarbon from the fractions with the temperature of more than 280 ℃ and the fractions with the temperature of less than 280 ℃ enter a catalytic cracking device together to produce gasoline with high octane number, and extract oil rich in aromatic hydrocarbon is used for aromatic hydrocarbon utilization; the HLCO in the method contains a large amount of bicyclic and tricyclic aromatic hydrocarbons, and the bicyclic and tricyclic aromatic hydrocarbons are directly discharged out of the device without being utilized, so that the overall economic benefit is poor.
In conclusion, in the existing method for processing poor diesel oil to obtain aromatic hydrocarbon or gasoline, the hydrocracking process can produce high-quality catalytic reforming raw materials and improve the quality of the diesel oil, but the investment is obviously larger; the solvent extraction process can improve the properties of poor diesel oil, but the utilization of the extracted aromatic hydrocarbon is not questioned; the combined hydro-reforming LCO-XTM process can only treat a small amount of LCO light fraction and is not suitable for large-scale processing; the hydrogenation-catalysis combined MGHC technology has good effect when the hydrofined LCO is processed independently, but if the hydrofined LCO is blended when the catalytic raw oil is processed, the cracking and the treatment capacity of the raw oil are obviously influenced, and BTX products cannot be produced by adopting the operation mode.
Disclosure of Invention
In order to solve the problem of high processing cost in the prior art of producing light aromatic hydrocarbon by using diesel oil, the invention provides a system for preparing light aromatic hydrocarbon from heavy oil raw material, which directly utilizes the prior catalytic cracking device to directly produce light aromatic hydrocarbon from heavy oil raw material, utilizes the prior equipment to the maximum extent, reduces the production cost, greatly reduces the hydrogen consumption, improves the yield of C6-C9 light aromatic hydrocarbon, and reduces the yield of diesel oil.
The technical scheme adopted by the invention to solve the technical problems is as follows: a system for preparing light aromatic hydrocarbons from heavy oil raw materials comprises a double-riser catalytic cracking device, a main fractionating tower, an auxiliary fractionating tower, a main cutting fractionating tower and an auxiliary cutting fractionating tower, wherein reaction oil gas generated by a heavy oil riser of the double-riser catalytic cracking device is sent into the main fractionating tower through a reaction oil-gas pipeline I for fractionation, catalytic cracking diesel oil generated by the fractionation of the main fractionating tower is sent into the main cutting fractionating tower through a catalytic cracking diesel oil pipeline for internal cutting, the generated light fraction I is sent into a reflux pipeline through a light fraction main pipeline, the generated heavy fraction I is sent into a main hydrogenation reactor through a heavy fraction main pipeline for primary hydrogenation, and the generated hydrogenated catalytic diesel oil is also sent into the reflux pipeline to be mixed with the light fraction I and sent into a second riser of the double-riser catalytic cracking device for secondary cracking reaction;
and reaction oil gas generated by the secondary cracking reaction is sent into an auxiliary fractionating tower through a reaction oil gas pipeline II for secondary fractionation, generated gasoline components enter a main gasoline pipeline, rich gas and sewage are separated through an oil-gas separator I and then sent into an auxiliary hydrogenation reactor for secondary hydrogenation, then the gasoline components are sent into an auxiliary cutting fractionating tower for cutting, generated light fraction II is discharged into a tank area through a light aromatic hydrocarbon pipeline for blending gasoline for use, and generated heavy fraction II is sent into an aromatic hydrocarbon combination device through a heavy fraction auxiliary pipeline to respectively generate C6-C9 light aromatic hydrocarbon products, raffinate gasoline products and heavy aromatic hydrocarbon products.
As an optimized scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, the gasoline component generated by fractionation of the main fractionating tower is introduced into the oil-gas separator II, and after rich gas and sewage are separated, the gasoline component is sent to the absorption tower through the auxiliary gasoline pipeline.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, the diesel fraction generated by secondary fractionation in the auxiliary fractionating tower is merged with the catalytic cracking diesel pipeline through the diesel pipeline and then is jointly sent to the main cutting fractionating tower.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, heavy oil slurry generated by fractionation of the main fractionation tower is divided into two paths through a circulating pipeline, one path of the heavy oil slurry reflows to the main fractionation tower, and the other path of the heavy oil slurry is sent to the auxiliary fractionation tower through a heavy oil pipeline I.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, the heavy oil generated by secondary fractionation in the secondary fractionating tower is returned to the circulating pipeline of the main fractionating tower through the heavy oil pipeline II.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, the reaction temperature in the heavy oil lifting pipe is 480-530 ℃, the catalyst-oil ratio is 4-8, the reaction pressure is 0.12-0.38 MPa, the reaction time is 2.2-4.5 s, and the atomized water vapor accounts for 4-8 wt% of the feeding amount.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, the feeding temperature of the main fractionating tower is 480-530 ℃, the bottom temperature of the tower is 350-420 ℃, the top temperature of the tower is 80-150 ℃ and the top pressure of the tower is 0.01-0.3 MPa.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, in the main cutting fractionating tower, the feeding temperature is 220-320 ℃, the bottom temperature is 100-350 ℃, the top temperature is 90-150 ℃ and the top pressure is 0.01-1 MPa, the light fraction I is obtained from the top of the tower, and the heavy fraction I is obtained from the bottom of the tower.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, in the main hydrogenation reactor, the reaction temperature of primary hydrogenation is 320-390 ℃, the hydrogen partial pressure is 5.0-10.0 MPa, the volume space velocity is 0.5-1.5 h < -1 >, and the hydrogen/oil volume ratio is 300-800.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, the reaction temperature of the secondary cracking reaction in the second lifting pipe is 560-630 ℃, the catalyst-oil ratio is 9-13, the reaction pressure is 0.12-0.38 MPa, the reaction time is 2.2-4.5 s, and the atomized water vapor accounts for 1.2-3.5 wt% of the feeding amount.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, the feeding temperature of the auxiliary fractionating tower is 450-530 ℃, the bottom temperature of the auxiliary fractionating tower is 250-350 ℃, the top temperature of the auxiliary fractionating tower is 80-150 ℃ and the top pressure of the auxiliary fractionating tower is 0.01-0.3 MPa.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, in the secondary hydrogenation reactor, the reaction temperature of secondary hydrogenation is 300-420 ℃, the hydrogen partial pressure is 2.5-3.5 MPa, the hydrogen/oil volume ratio is 500-800, and the volume space velocity is 1.5-4 h < -1 >.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, the feeding temperature of the auxiliary cutting fractionating tower is 50-90 ℃, the tower bottom temperature is 100-150 ℃, the tower top temperature is 40-80 ℃ and the tower top pressure is 0.01-0.3 MPa.
As another optimization scheme of the system for preparing the light aromatic hydrocarbon from the heavy oil raw material, in the aromatic hydrocarbon combination device, the tower top temperature of an extraction tower used for extracting the aromatic hydrocarbon is 130-190 ℃, and the pressure is 1.0-2.0 MPa.
Compared with the prior art, the invention has the following beneficial effects:
1) The method utilizes the existing hydrogenation equipment and catalytic cracking device to the maximum extent, reduces the investment and operation cost of the equipment, heavy oil raw materials are firstly subjected to primary catalytic cracking in a heavy oil lifting pipe, then gasoline fraction and catalytic cracking diesel fraction are fractionated in a main fractionating tower, catalytic cracking diesel is cut in the main cutting fractionating tower to form light fraction and heavy fraction, the heavy fraction is subjected to primary hydrogenation in a main hydrogenation reactor and then is mixed with the light fraction to be sent into a second lifting pipe for secondary catalytic cracking, reaction oil gas at the moment is fractionated into gasoline and diesel oil in an auxiliary fractionating tower, the diesel oil component returns to the main cutting fractionating tower to continue reacting, the gasoline component enters the auxiliary cutting fractionating tower to be cut after secondary hydrogenation reaction in the auxiliary hydrogenation reactor, the light fraction and the heavy fraction are separated, the heavy fraction is finally sent into an aromatic hydrocarbon combination device, and three products of light aromatic hydrocarbon, raffinate gasoline and heavy aromatic hydrocarbon are separated; in the whole system, the diesel oil generated by heavy oil catalytic cracking needs to be subjected to secondary catalytic cracking and secondary hydrogenation, so that the hydrogenation pressure is reduced, the hydrogen consumption is obviously reduced (compared with the technology for producing BTX raw material by hydrocracking, the hydrogen consumption of the process can be reduced from more than 4wt% to less than 2.0wt%, and the hydrogenation pressure can be reduced from 12MPa to about 7 MPa), and the yield of C6-C9 aromatic hydrocarbon in the final product can reach more than 50 wt%;
2) According to the invention, the poor diesel oil generated by heavy oil catalytic cracking is separated into two parts of 'saturated hydrocarbon + monocyclic aromatic hydrocarbon' and bicyclic and above aromatic hydrocarbons, and the bicyclic and above aromatic hydrocarbons are used for producing the monocyclic aromatic hydrocarbons through a hydrogenation process, so that on one hand, the increase of hydrogen consumption of a device caused by the circulation of the saturated hydrocarbon and the monocyclic aromatic hydrocarbons in a hydrogenation device is avoided, and on the other hand, the bicyclic aromatic hydrocarbons in the poor diesel oil are subjected to hydrogenation saturation into the monocyclic aromatic hydrocarbons in a targeted manner, so that the hydrogenation efficiency is improved, and simultaneously, the hydrogen consumption is further reduced;
3) The second riser of the double-riser catalytic cracking device is used for cracking the hydrocatalytic diesel oil and the light fraction, so that the operation cost of producing aromatic hydrocarbon by the diesel oil is obviously reduced, and the process economy is improved;
4) The invention uses the existing diesel hydrogenation-catalytic cracking process as the basis, carries out process transformation on the basis, firstly cuts and then carries out secondary hydrogenation, uses the inferior diesel to produce light aromatic products with high added value, can solve the problem of the poor diesel of refineries when improving the economic benefit, and has obvious economic and social benefits.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
FIG. 2 is a schematic process flow diagram of comparative example 1;
FIG. 3 is a schematic process flow diagram of comparative example 2;
reference numerals: 1. the heavy oil riser comprises a heavy oil riser, 2, a second riser, 3, reaction oil and gas pipelines I and 4, a main fractionating tower and 5, a catalytic cracking diesel oil pipeline, 6, a main cutting fractionating tower and 7, a heavy fraction main pipeline and 8, a light fraction main pipeline and 9, a main hydrogenation reactor, 10, a backflow pipeline and 11, reaction oil and gas pipelines II and 12, an auxiliary fractionating tower and 13, oil and gas separators I and 14, a main gasoline pipeline and 15, an auxiliary hydrogenation reactor and 16, an auxiliary cutting fractionating tower and 17, a heavy fraction auxiliary pipeline and 18, an aromatic hydrocarbon combination device and 19, a light fraction auxiliary pipeline and 20, a diesel oil pipeline and 21, an oil and gas separator II and 22, an auxiliary gasoline pipeline and 23, heavy oil pipelines I and 24, a circulating pipeline and 25 and a heavy oil pipeline II.
Detailed Description
The technical scheme of the present invention is further described in detail with reference to the following specific examples, and the parts of the present invention not described in the following examples are all the prior art, such as the selection of the catalyst used in catalytic cracking, the structure of an oil-gas separator, the structure of an aromatics complex, the structure of a hydrogenation reactor, the structure of a cutting splitting tower, the structure of a fractionating tower, and the like.
Example 1
A system for preparing light aromatic hydrocarbon from poor diesel oil comprises a double-riser catalytic cracking device, a main fractionating tower 4, an auxiliary fractionating tower 12, a main cutting fractionating tower 6 and an auxiliary cutting fractionating tower 16, wherein poor diesel oil raw materials enter a heavy oil riser 1 of the double-riser catalytic cracking device to perform primary catalytic cracking reaction, the reaction temperature of primary catalytic cracking is 480-530 ℃, the catalyst-oil ratio is 4-8, the reaction pressure is 0.12-0.38 MPa, the reaction time is 2.2-4.5 s, atomized water vapor accounts for 4-8 wt% of the feeding amount, reaction oil gas generated by the reaction is settled through a main settler and then is fed into the main fractionating tower 4 through a reaction oil-gas pipeline I3 for fractionation, the feeding temperature during fractionation is 480-530 ℃, the bottom temperature is 350-420 ℃, the top temperature is 80-150 ℃ and the top pressure is 0.01-0.3 MPa, three fractions are generated through fractionation, namely a gasoline component, catalytic cracking diesel oil and a heavy oil slurry, wherein the catalytic cracking diesel oil generated by the main fractionating tower 4 is fed into the main cracking pipeline 5-6 ℃ and the top temperature fractionation tower, the bottom temperature is 100.01-100 ℃ and the heavy oil slurry is obtained from the main fractionating tower, the top temperature fractionation tower, the top temperature is 100-100 ℃ and the bottom temperature is cut from the top temperature I; the produced light fraction I is sent into a reflux pipeline 10 through a light fraction main pipeline 8, the produced heavy fraction I is sent into a main hydrogenation reactor 9 through a heavy fraction main pipeline 7 for primary hydrogenation, the reaction temperature of the primary hydrogenation is 320-390 ℃, the hydrogen partial pressure is 5.0-10.0 MPa, the volume space velocity is 0.5-1.5 h < -1 >, and the hydrogen/oil volume ratio is 300-800; the hydrocatalytic diesel oil generated by the primary hydrogenation is also sent into a reflux pipeline 10 to be mixed with the light fraction I, and then is sent into a second lifting pipe 2 of the double lifting pipe catalytic cracking device together for secondary cracking reaction, wherein the reaction temperature of the secondary cracking reaction is 560-630 ℃, the catalyst-oil ratio is 9-13, the reaction pressure is 0.12-0.38 MPa, the reaction time is 2.2-4.5 s, and the atomized water vapor accounts for 1.2-3.5 wt% of the feeding amount;
reaction oil gas generated by secondary cracking reaction is settled by a secondary settler and then sent into a secondary fractionating tower 12 through a reaction oil gas pipeline II 11 for secondary fractionation, the feeding temperature of the secondary fractionation is 450-530 ℃, the bottom temperature of the tower is 250-350 ℃, the top temperature of the tower is 80-150 ℃, the top pressure of the tower is 0.01-0.3 MPa, three parts, namely a gasoline component, a diesel component and a heavy oil slurry, are generated by fractionation, wherein the generated gasoline component enters a main gasoline pipeline 14, rich gas and sewage are separated by an oil-gas separator I13 and then sent into a secondary hydrogenation reactor 15 for secondary hydrogenation, the reaction temperature of the secondary hydrogenation is 300-420 ℃, the hydrogen partial pressure is 2.5-3.5 MPa, the hydrogen/oil volume ratio is 500-800 1, and the volume space velocity is 1.5-4 h < -1 >; and after secondary hydrogenation, the mixture is sent into an auxiliary cutting fractionating tower 16 for cutting, the feeding temperature in the auxiliary cutting fractionating tower 16 is 50-90 ℃, the tower bottom temperature is 100-150 ℃, the tower top temperature is 40-80 ℃ and the tower top pressure is 0.01-0.3 MPa, light fraction II and heavy fraction II are generated through cutting, the generated light fraction II is mainly C5C6 alkane and is discharged to a tank area through a light fraction auxiliary pipeline 19 for blending gasoline use, the generated heavy fraction II is sent into an aromatic hydrocarbon combination device 18 through a heavy fraction auxiliary pipeline 17, the aromatic hydrocarbon combination device 18 is used, the tower top temperature of an extraction tower for aromatic hydrocarbon extraction is 130-190 ℃, the pressure is 1.0-2.0 MPa, C6-C9 light aromatic hydrocarbon products, raffinate gasoline products and heavy aromatic hydrocarbon products are generated respectively, and the raffinate gasoline and heavy aromatic hydrocarbon are sent to a gasoline pool for blending gasoline use.
The process route of the embodiment is that raw materials are subjected to primary catalytic cracking reaction in a heavy oil riser 1 of a double-riser catalytic cracking device, generated product reaction oil gas enters a main fractionating tower 4 through a first reaction oil gas pipeline 3 for fractionation, catalytic cracking diesel oil generated by fractionation enters a main cutting fractionating tower 6 through a catalytic cracking diesel oil pipeline 5, after the catalytic cracking diesel oil is cut and fractionated by the main cutting fractionating tower 6, light fractions are sent into a reflux pipeline 10 through a light fraction main pipeline 8 and returned into a second riser 2 of the double-riser catalytic cracking device through the reflux pipeline 10, heavy fractions are sent into a main hydrogenation reactor 9 through a heavy fraction main pipeline 7 for primary hydrogenation, and generated hydrogenation catalytic diesel oil is returned into the second riser 2 of the double-riser catalytic cracking device through the reflux pipeline 10 for secondary cracking reaction;
reaction oil gas generated in the second lifting pipe 2 enters an auxiliary fractionating tower 12 through a second reaction oil gas pipeline 11 for fractionation, gasoline components generated after fractionation enter an auxiliary hydrogenation reactor 15 through a main gasoline pipeline 14 for secondary hydrogenation, then are sent to an auxiliary cutting fractionating tower 16 for cutting and fractionation, generated light fractions are discharged to a tank area through a light fraction auxiliary pipeline 19 for blending with gasoline for use, and heavy fractions are sent to an aromatic hydrocarbon combination device 18 through a heavy fraction auxiliary pipeline 17 to generate three products (C6-C9 light aromatic hydrocarbon, raffinate gasoline and heavy aromatic hydrocarbon);
diesel oil produced by the fractionation of the auxiliary fractionating tower 12 enters the main cutting fractionating tower 6 through a diesel oil pipeline 20;
the light fraction produced by fractionation in the main column 4 is the gasoline component and is sent to the absorber via the secondary gasoline line 22.
Example 2
This embodiment is a limited scheme of embodiment 1, and the main structure thereof is the same as that of embodiment 1, and the limited part is as follows: and gasoline components produced by fractionation of the main fractionating tower 4 are introduced into the oil-gas separator II 21, and after rich gas and sewage are separated, the gasoline components are sent to the absorption tower through the auxiliary gasoline pipeline 22.
Example 3
This embodiment is another limitation to embodiment 1, and the main structure thereof is the same as embodiment 1, and the limitation lies in: the diesel oil fraction generated by the secondary fractionation in the secondary fractionating tower 12 is merged with the catalytic cracking diesel oil pipeline 5 through the diesel oil pipeline 20 and then is sent to the main cutting fractionating tower 6 together.
Example 4
The present embodiment is another limiting scheme performed on embodiment 1, and the main structure of the present embodiment is the same as that of embodiment 1, and the limiting part is as follows: heavy oil slurry generated by fractionation of the main fractionating tower 4 is divided into two paths through a circulating pipeline 24, one path reflows to the main fractionating tower 4, and the other path is sent to the auxiliary fractionating tower 12 through a heavy oil pipeline I23.
Example 5
This embodiment is another limitation to embodiment 1, and the main structure thereof is the same as embodiment 1, and the limitation lies in: the heavy oil produced by the secondary fractionation in the secondary fractionator 12 is returned to the recycle line 24 of the main fractionator 4 via the heavy oil line ii 25.
In order to verify the advantages of the present invention compared to the prior art, the process equipment of the present invention was used to perform the following detection and comparison experiments.
Detection experiment
The detection experiment adopts the equipment of FIG. 1, and the specific process flow is as follows:
1) Introducing a heavy oil raw material into a heavy oil riser 1 to perform catalytic cracking reaction, feeding reaction oil gas into a main fractionating tower 4 to perform fractionation, directly feeding a fractionated gasoline component into an absorption tower, feeding a fractionated catalytic cracking diesel oil component (the component properties of the catalytic cracking diesel oil component are shown in table 1) into a main cutting fractionating tower 6, and obtaining a light fraction from the top of the tower and a heavy fraction from the bottom of the tower at a feeding temperature of 220 ℃, a bottom temperature of 300 ℃, a top temperature of 240 ℃ and a top pressure of 0.01 MPa;
2) Sending the heavy fraction obtained in the step 1) into a main hydrogenation reactor 9 for primary hydrogenation reaction to saturate polycyclic aromatic hydrocarbons in the heavy fraction into monocyclic aromatic hydrocarbons, thereby obtaining hydrogenation catalytic diesel oil;
the reaction temperature of the primary hydrogenation reaction is 390 ℃, the hydrogen partial pressure is 10.0MPa, the volume space velocity is 2.5h < -1 >, the hydrogen/oil volume ratio is 800;
3) Combining the hydrocatalytic diesel oil obtained in the step 2) and the light fraction obtained in the step 1), and then sending the mixture into a second riser 2 for secondary cracking, sending reaction oil gas generated by secondary cracking into an auxiliary fractionating tower 12 for fractionating cracked gasoline and cracked diesel oil, and sending the cracked diesel oil back into a main cutting fractionating tower 6;
the reaction temperature of the secondary cracking in the second lifting pipe 2 is 600 ℃, the catalyst-oil ratio is 14, the reaction pressure is 0.3Mpa, the reaction time is 4s, and the atomized water vapor accounts for 1wt% of the feeding amount;
4) Feeding the cracked gasoline fractionated in the step 3) into an auxiliary hydrogenation reactor 15 for secondary hydrogenation reaction to obtain refined gasoline, and performing cutting fractionation in an auxiliary cutting fractionating tower 16 at 75 ℃ serving as a cutting point to obtain heavy fraction larger than the cutting point and light aromatic hydrocarbon smaller than the cutting point, wherein the light fraction is used as a gasoline blending product;
in the step, the reaction temperature of the secondary hydrogenation reaction is 420 ℃, the hydrogen partial pressure is 3.5MPa, the hydrogen/oil volume ratio is 500:1, the volume space velocity is 4h < -1 >, and the catalyst is a cobalt-molybdenum catalyst, and the addition amount of the cobalt-molybdenum catalyst is 6wt%;
5) Sending the heavy fraction obtained in the step 4) into an aromatic hydrocarbon combination device 18, and performing aromatic hydrocarbon extraction and aromatic hydrocarbon fractionation on the heavy fraction by the aromatic hydrocarbon combination device 18 to obtain a C6-C9 light aromatic hydrocarbon product, raffinate gasoline and heavy aromatic hydrocarbon components, wherein the raffinate gasoline and the heavy aromatic hydrocarbon components are used as gasoline blending products;
in the step, during the extraction of the aromatic hydrocarbon, the extraction solvent is sulfolane, and the mass ratio of the extraction solvent to the heavy fraction is 8; the temperature of the top of the extraction tower used for extracting the aromatic hydrocarbon is 190 ℃, and the pressure is 2.0MPa.
The total process hydrogen consumption and product distribution in this test are shown in table 2.
TABLE 1 catalytic cracking Diesel Properties
TABLE 2 Total Process Hydrogen consumption and product distribution
Comparative example 1
The catalytic cracking diesel oil used in the comparative example was obtained from diesel oil produced by catalytic cracking of a heavy oil feedstock in a test experiment, as shown in table 1, using a process scheme as shown in fig. 2. The difference from the detection experiment lies in that the catalytic diesel oil which is catalytically cracked by the heavy oil lifting pipe 1 is not subjected to fractionation by the main fractionating tower 4 and cutting by the main cutting fractionating tower 6, is completely subjected to hydrofining in the main hydrogenation reactor 9, then is subjected to secondary cracking in the second lifting pipe 2, and the reaction oil gas is not subjected to fractionation by the auxiliary fractionating tower 12, is directly sent to the auxiliary hydrogenation reactor 15 for secondary hydrogenation, and then is subjected to cutting fractionation by the auxiliary cutting fractionating tower 16 and extraction and fractionation by the aromatic hydrocarbon combination device 18 to obtain a product;
the reaction conditions of the main hydrogenation reactor 9 are the same as those of the detection experiment, the reaction parameters of the second lifting pipe 2 during cracking are the same as those of the detection experiment, the reaction parameters of the auxiliary hydrogenation reactor 15 are the same as those of the detection experiment, the parameters of the auxiliary cutting fractionating tower 16 and the arene combination device 18 are the same as those of the detection experiment, and the obtained hydrogen consumption and product distribution of the whole process are shown in table 2.
Comparative example 2
The catalytically cracked diesel oil used in this comparative example was obtained from diesel oil produced by catalytic cracking of a heavy oil feedstock in a test experiment, as shown in Table 1, using the process flow shown in FIG. 3. The difference from the detection experiment lies in that catalytic diesel oil which is catalytically cracked by a heavy oil riser 1 is directly introduced into an auxiliary hydrogenation reactor 15 for hydrogenation, and then is subjected to cutting fractionation in an auxiliary cutting fractionating tower 16 and aromatic extraction and fractionation in an aromatic combination device 18 to obtain a product, wherein the reaction parameters of the auxiliary hydrogenation reactor 15, the auxiliary cutting fractionating tower 16 and the aromatic combination device 18 are the same as those in the detection experiment, and the obtained total process hydrogen consumption and product distribution are shown in table 2.
As can be seen from the comparison of the data in Table 2, the hydrogen consumption of the detection experiment can be reduced to below 2wt%, the total yield of benzene, toluene, xylene and trimethylbenzene can reach above 50wt%, the hydrogen consumption of the comparative example 1 is 4.16wt%, and the hydrogen consumption of the comparative example 2 is 4.20wt%, that is, the process of the invention not only reduces the hydrogenation pressure, but also obviously reduces the hydrogen consumption.
Although specific embodiments of the present invention have been described above, it will be appreciated by those skilled in the art that these are merely illustrative and that many changes and modifications may be made to the embodiments without departing from the principles and spirit of the invention, the scope of which is defined solely by the appended claims.
Claims (14)
1. The system for preparing light aromatic hydrocarbon from heavy oil raw material comprises a double-riser catalytic cracking device, a main fractionating tower (4), an auxiliary fractionating tower (12), a main cutting fractionating tower (6) and an auxiliary cutting fractionating tower (16), and is characterized in that: reaction oil gas generated by a heavy oil riser (1) of the double-riser catalytic cracking device is sent into a main fractionating tower (4) through a reaction oil gas pipeline I (3) for fractionation, catalytic cracking diesel oil generated by fractionation of the main fractionating tower (4) is sent into a main cutting fractionating tower (6) through a catalytic cracking diesel oil pipeline (5) for internal cutting, generated light fraction I is sent into a return pipeline (10) through a light fraction main pipeline (8), generated heavy fraction I is sent into a main hydrogenation reactor (9) through a heavy fraction main pipeline (7) for primary hydrogenation, and generated hydrocatalytic diesel oil is also sent into the return pipeline (10) to be mixed with the light fraction I and sent into a second riser (2) of the double-riser catalytic cracking device for secondary cracking reaction;
reaction oil gas generated by secondary cracking reaction is sent into an auxiliary fractionating tower (12) through a reaction oil gas pipeline II (11) for secondary fractionation, generated gasoline components enter a main gasoline pipeline (14), rich gas and sewage are separated through an oil-gas separator I (13) and then sent into an auxiliary hydrogenation reactor (15) for secondary hydrogenation, then sent into an auxiliary cutting fractionating tower (16) for cutting, generated light fraction II is discharged into a tank area through a light fraction auxiliary pipeline (19) for blending gasoline, and generated heavy fraction II is sent into an aromatic hydrocarbon combination device (18) through a heavy fraction auxiliary pipeline (17) to respectively generate C6-C9 light aromatic hydrocarbon products, raffinate gasoline products and heavy aromatic hydrocarbon products.
2. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: and gasoline components generated by fractionation of the main fractionating tower (4) are introduced into an oil-gas separator II (21), and rich gas and sewage are separated and then are sent to the absorption tower through an auxiliary gasoline pipeline (22).
3. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: and diesel fractions generated by secondary fractionation in the auxiliary fractionating tower (12) are merged with the catalytic cracking diesel pipeline (5) through the diesel pipeline (20) and then are jointly sent to the main cutting fractionating tower (6).
4. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: heavy oil slurry generated by fractionation of the main fractionating tower (4) is divided into two paths through a circulating pipeline (24), one path of heavy oil slurry reflows to the main fractionating tower (4), and the other path of heavy oil slurry is sent to the auxiliary fractionating tower (12) through a heavy oil pipeline I (23).
5. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: heavy oil generated by the secondary fractionation in the secondary fractionating tower (12) is returned to the circulating pipeline (24) of the main fractionating tower (4) through a heavy oil pipeline II (25).
6. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: the reaction temperature in the heavy oil lifting pipe (1) is 480-530 ℃, the catalyst-oil ratio is 4-8, the reaction pressure is 0.12-0.38 MPa, the reaction time is 2.2-4.5 s, and the atomized water vapor accounts for 4-8 wt% of the feeding amount.
7. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: the feeding temperature of the main fractionating tower (4) is 480-530 ℃, the bottom temperature is 350-420 ℃, the top temperature is 80-150 ℃ and the top pressure is 0.01-0.3 MPa.
8. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: in the main cutting fractionating tower (6), the feeding temperature is 220-320 ℃, the bottom temperature is 100-350 ℃, the top temperature is 90-150 ℃ and the top pressure is 0.01-1 MPa, so that the light fraction I is obtained from the top of the tower, and the heavy fraction I is obtained from the bottom of the tower.
9. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: in the main hydrogenation reactor (9), the reaction temperature of primary hydrogenation is 320-390 ℃, the hydrogen partial pressure is 5.0-10.0 MPa, and the volume space velocity is 0.5-1.5 h -1 The hydrogen/oil volume ratio is 300 to 800.
10. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: the reaction temperature of the second cracking reaction in the second riser (2) is 560-630 ℃, the catalyst-oil ratio is 9-13, the reaction pressure is 0.12-0.38 MPa, the reaction time is 2.2-4.5 s, and the atomized water vapor accounts for 1.2-3.5 wt% of the feeding amount.
11. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: the feeding temperature of the auxiliary fractionating tower (12) is 450-530 ℃, the bottom temperature of the tower is 250-350 ℃, the top temperature of the tower is 80-150 ℃, and the top pressure of the tower is 0.01-0.3 MPa.
12. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: in the secondary hydrogenation reactor (15), the reaction temperature of secondary hydrogenation is 300-420 ℃, the hydrogen partial pressure is 2.5-3.5 MPa, the hydrogen/oil volume ratio is 500-800, and the volume space velocity is 1.5-4 h -1 。
13. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: the feeding temperature of the auxiliary cutting fractionating tower (16) is 50-90 ℃, the bottom temperature of the tower is 100-150 ℃, the top temperature of the tower is 40-80 ℃, and the top pressure of the tower is 0.01-0.3 MPa.
14. The system for preparing light aromatic hydrocarbons from heavy oil raw materials according to claim 1, wherein: in the aromatic hydrocarbon combination device (18), the temperature of the top of the extraction tower used for extracting the aromatic hydrocarbon is 130-190 ℃, and the pressure is 1.0-2.0 MPa.
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| CN116355649A (en) * | 2023-04-14 | 2023-06-30 | 中国石油化工股份有限公司 | Device and method for producing light aromatic hydrocarbon and heavy aromatic hydrocarbon |
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