CN117660049A - Hydrogenation method for producing BTX - Google Patents
Hydrogenation method for producing BTX Download PDFInfo
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- CN117660049A CN117660049A CN202211016689.8A CN202211016689A CN117660049A CN 117660049 A CN117660049 A CN 117660049A CN 202211016689 A CN202211016689 A CN 202211016689A CN 117660049 A CN117660049 A CN 117660049A
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 title abstract description 11
- 238000006243 chemical reaction Methods 0.000 claims abstract description 99
- 238000000034 method Methods 0.000 claims abstract description 50
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 46
- 239000003054 catalyst Substances 0.000 claims abstract description 43
- 239000002283 diesel fuel Substances 0.000 claims abstract description 30
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 19
- 239000001257 hydrogen Substances 0.000 claims abstract description 17
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 17
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- 238000004523 catalytic cracking Methods 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims abstract description 11
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- 230000003197 catalytic effect Effects 0.000 claims description 26
- 230000008569 process Effects 0.000 claims description 20
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 238000005336 cracking Methods 0.000 claims description 8
- 229910052751 metal Inorganic materials 0.000 claims description 8
- 239000002184 metal Substances 0.000 claims description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- 239000011230 binding agent Substances 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052721 tungsten Inorganic materials 0.000 claims description 3
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 2
- 239000010941 cobalt Substances 0.000 claims description 2
- 229910017052 cobalt Inorganic materials 0.000 claims description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 2
- 229910052750 molybdenum Inorganic materials 0.000 claims description 2
- 239000011733 molybdenum Substances 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical group [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 2
- 239000010937 tungsten Substances 0.000 claims description 2
- 238000009835 boiling Methods 0.000 claims 1
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- 150000002431 hydrogen Chemical class 0.000 description 10
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 125000003118 aryl group Chemical group 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- -1 dicyclic aromatic hydrocarbon Chemical class 0.000 description 5
- 238000004821 distillation Methods 0.000 description 5
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- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
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- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 3
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- UWHCKJMYHZGTIT-UHFFFAOYSA-N Tetraethylene glycol, Natural products OCCOCCOCCOCCO UWHCKJMYHZGTIT-UHFFFAOYSA-N 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
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- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a hydrogenation method for producing BTX, which comprises the following steps: (1) Cutting the catalytic cracking diesel oil to obtain light and heavy distillate oil, wherein the cutting point is 300-350 ℃, preferably 310-330 ℃; (2) The light distillate oil obtained in the step (1) enters a hydrofining reaction zone to carry out hydrofining reaction under the action of a hydrofining catalyst; (3) The reaction material after hydrofining in the step (2) enters a hydrocracking reaction zone to carry out hydrocracking reaction under the action of a hydrocracking catalyst; (4) And (3) feeding the hydrocracking generated oil obtained in the step (3) into a separation system for gas-liquid separation, recycling the separated gas as supplementary hydrogen, further separating the liquid phase product to obtain light naphtha, heavy naphtha and tail oil, and extracting the heavy naphtha by aromatic hydrocarbon to obtain BTX. The method can effectively improve the BTX yield of the hydroconversion device, reduce the operation severity of the device and prolong the operation period of the device.
Description
Technical Field
The invention relates to a hydrogenation method for producing BTX, in particular to a hydrogenation method for producing BTX with long period and high yield by taking catalytic diesel oil as a raw material.
Background
Light aromatic hydrocarbons such as Benzene (Benzene), toluene (Tolene), xylene (Xylene) are important basic chemical raw materials. With the industrial development and the improvement of the human living standard, the industrial development of synthetic fibers, synthetic plastics and synthetic rubber is rapid, the demand for BTX is growing year by year, and the current situation of supply and demand is present. The hydrocracking process is adopted to convert the dicyclic aromatic hydrocarbon in the catalytic diesel oil into light aromatic hydrocarbon (such as BTX and the like), and is an ideal way for solving the problems of excessive diesel oil and shortage of low-carbon aromatic hydrocarbon. In the hydrocracking process, the dicyclic arene is first hydrogenated to produce tetrahydronaphthalene compound, and then ring opened and side chain broken to produce short side chain BTX arene.
CN201510761954.9 discloses a hydrocracking catalyst grading method and a catalytic diesel hydrogenation conversion process. The grading method comprises the following steps: the hydrocracking reactor is equally divided into 2-8 reaction areas along the material flow direction, the hydrocracking catalyst containing the regenerant is filled in each reaction area, the content of the regenerant in the hydrocracking catalyst is 10-90 wt% based on the weight of the hydrocracking catalyst, and the content of the regenerant in the hydrocracking catalyst in each reaction area along the material flow direction is gradually increased. The invention also provides a catalytic diesel oil hydro-conversion process comprising the hydrocracking catalyst grading method. By grading and filling catalysts with different reaction performances in the cracking reactor, the hydrogenation selectivity of diesel oil/gasoline components in the conversion process is improved, and the yield of high-octane gasoline products is improved.
CN201711118958.0 discloses a method for producing high-quality gasoline and diesel oil by catalyzing diesel oil, comprising the following steps: (1) Mixing high aromatic catalytic diesel oil and circulating hydrogen, and entering an I hydrofining reaction zone for reaction; (2) The generated oil obtained in the step (1) and the recycle hydrogen are mixed and enter a hydrofining reaction zone II for reaction, wherein the reaction temperature is 30-120 ℃ higher than that of the hydrofining reaction zone I; (3) Cutting the generated oil obtained in the step (2) into a light component and a heavy component; (4) Mixing the light component obtained in the step (3) with recycle hydrogen, entering a hydro-upgrading reaction zone, and separating generated oil to obtain gasoline fraction and diesel fraction; (5) Mixing the heavy component obtained in the step (3) with circulating hydrogen, entering a hydro-conversion reaction zone, generating oil, passing through a separation system, obtaining gas, gasoline and diesel oil fractions, (6) mixing the gasoline obtained in the step (4) with the gasoline obtained in the step (5) to obtain a qualified gasoline product, and mixing the diesel oil obtained in the step (4) with the diesel oil obtained in the step (5) to obtain a qualified diesel oil product. The method can produce high-quality fuel oil products, and has the characteristics of low chemical hydrogen consumption and flexible structure adjustment compared with other technologies.
CN201711118979.2 discloses a method for catalyzing the hydroconversion of diesel oil, comprising the following steps: (1) Mixing high aromatic catalytic diesel oil and circulating hydrogen, and entering an I hydrofining reaction zone for reaction; (2) The generated oil obtained in the step (1) and the circulating hydrogen are mixed and enter a hydrofining reaction zone II for further reaction, the reaction temperature is 30-120 ℃ higher than that of the hydrofining reaction zone I, and the liquid time volume air-conditioner is 0.2-1.5 h < -1 > lower than that of the hydrofining reaction zone I; (3) The generated oil obtained in the step (2) and the recycle hydrogen are mixed and enter a hydrocracking reaction zone for hydrocarbon hydrogenation conversion reaction; (4) And (3) separating and fractionating the generated oil obtained in the step (3) to obtain gas, light naphtha, heavy naphtha and diesel fraction, recycling part of diesel to the II hydrofining reaction zone, and discharging part of diesel from the device. The catalytic diesel hydrogenation conversion method provided by the method can effectively increase aromatic hydrocarbon.
The invention discloses a method for producing high-quality gasoline by catalyzing diesel oil hydrogenation conversion, which comprises the following steps: (1) Mixing high aromatic catalytic diesel oil and circulating hydrogen, and allowing the mixture to enter a hydrofining reaction zone for reaction, wherein the hydrofining reaction zone is provided with at least two catalyst beds, and the sulfidation degree of the catalyst is reduced along the material flow direction; (2) The generated oil obtained in the step (1) enters a hydrocracking reaction zone to contact with at least two sulfuration hydrocracking catalysts to carry out ring-opening conversion reaction of polycyclic aromatic hydrocarbon; (3) And (3) the generated oil obtained in the step (2) passes through a separation system to obtain gas, gasoline and diesel fractions. The method solves the problems of long initial adjustment period and long-time low octane number of the main target product gasoline fraction in the production process.
CN201611045476.2 discloses a catalytic diesel processing method. Cutting the catalytic diesel raw material into light components and heavy components; carrying out hydrofining and hydro-upgrading reaction on the light component to obtain gasoline and diesel components; hydrofining and hydroconverting the heavy component to obtain a gasoline component and a diesel component; the two parts of gasoline and diesel components are mixed to obtain a gasoline product, and the two parts of diesel components are mixed to obtain a diesel product. The invention can carry out selective independent processing aiming at different types of raw materials through reasonable separation and processing processes, thereby reasonably utilizing poor catalytic cracking diesel oil to produce qualified gasoline and diesel oil products.
CN201310540464.7 discloses a catalytic cracking diesel hydro-conversion method. After the catalytic diesel oil is mixed with hydrogen, a hydrofining reactor is first used for hydrofining reaction; the effluent of the hydrofining reaction directly enters a hydrocracking reactor to contact and react with a graded catalyst bed in the hydrocracking reactor; at least two cracking catalyst beds are arranged in the hydrocracking reactor, and the hydrogenation activity of the hydrocracking catalyst is reduced according to the flow direction of reaction materials; and separating and fractionating the hydrocracking reaction effluent to obtain naphtha and diesel oil. The method can reduce excessive hydrogenation and secondary cracking of the cracked naphtha while ensuring the hydrocracking effect of the diesel, and reduce the chemical hydrogen consumption, thereby improving the octane number and the liquid yield of the naphtha.
CN201811264066.6 discloses a method for producing aromatic hydrocarbons in maximum amount by catalytic diesel oil hydroconversion, comprising the following steps: (1) Mixing high aromatic catalytic diesel oil and circulating hydrogen, and allowing the mixture to enter a hydrofining reaction zone for reaction, wherein the hydrofining reaction zone is provided with at least two catalyst beds, and the sulfidation degree of the catalyst is reduced along the material flow direction; (2) The generated oil obtained in the step (1) enters a hydrocracking reaction zone to contact with at least two sulfuration hydrocracking catalysts to carry out ring-opening conversion reaction of polycyclic aromatic hydrocarbon; (3) The generated oil obtained in the step (2) is subjected to a separation system to obtain gas, gasoline and diesel oil fractions, and the diesel oil fractions are all circulated back to the hydrofining reaction zone; (4) And (3) feeding the naphtha obtained in the step (3) into an aromatic hydrocarbon extraction device, and extracting with a solvent to obtain a BTX product. The invention balances the initial activity of the catalyst by grading hydrogenation catalysts with different sulfuration degrees, and solves the problems of long initial adjustment period and long-time low octane number of the main target product gasoline fraction in the technical application process.
In the prior art, the problems of low BTX product yield and short operation period of a hydroconversion device are commonly existed in the process of catalyzing diesel hydroconversion. How to develop a catalytic diesel hydro-conversion process with high yield of BTX products and to prolong the running period of the device is a problem to be solved.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a hydrogenation method for producing BTX, which can effectively improve the BTX yield of a hydroconversion device, reduce the operation severity of the device and prolong the operation period of the device.
A hydrogenation process for producing BTX, the process comprising the steps of:
(1) Cutting the catalytic cracking diesel oil to obtain light and heavy distillate oil, wherein the cutting point is 300-350 ℃, preferably 310-330 ℃;
(2) The light distillate oil obtained in the step (1) enters a hydrofining reaction zone to carry out hydrofining reaction under the action of a hydrofining catalyst;
(3) The reaction material after hydrofining in the step (2) enters a hydrocracking reaction zone to carry out hydrocracking reaction under the action of a hydrocracking catalyst;
(4) And (3) feeding the hydrocracking generated oil obtained in the step (3) into a separation system for gas-liquid separation, recycling the separated gas as supplementary hydrogen, further separating the liquid phase product to obtain light naphtha, heavy naphtha and tail oil, and extracting the heavy naphtha by aromatic hydrocarbon to obtain BTX.
In the method, the initial distillation point of the catalytic diesel in the step (1) is generally 60-220 ℃, preferably 170-210 ℃; the density is generally 0.90g/cm -3 ~0.99 g/cm -3 The method comprises the steps of carrying out a first treatment on the surface of the The nitrogen content is generally 0.03-0.2 m%; the aromatic hydrocarbon content is generally 50-90 m%, preferably 65-85 m%.
In the method, the mass content of the tricyclic aromatic hydrocarbon in the light distillate oil obtained in the step (1) is 0.1% -5%, preferably 0.2% -4%, and more preferably 1% -3% or more; the nitrogen content is 100mg/kg to 500mg/kg, preferably 200mg/kg to 300mg/kg.
The method, wherein the hydrofining catalyst in the step (2) comprises a carrier and hydrogenation active metal; wherein the carrier is inorganic refractory oxide, and is generally selected from one or more of alumina, amorphous silica-alumina, silicon dioxide or titanium oxide; the hydrogenation active metal comprises a group VIB and/or group VIII metal component, wherein the group VIB in the hydrofining catalyst is selected from tungsten and/or molybdenum, the content of the group VIB in the catalyst is 5-30 percent, preferably 10-20 percent, based on the oxidation mass, and the content of the group VIII in the catalyst is selected from nickel and/or cobalt, preferably 1.5-5 percent, based on the oxidation mass.
In the method, compared with the process conditions that catalytic diesel is directly subjected to hydroconversion without cutting treatment, the reaction conditions of the hydrofining reaction zone in the step (2) are as follows: the reaction pressure is lower by 0.5-6.0 MPa, preferably 1.0-3.0 MPa; the average temperature is 5-30 ℃, preferably 10-20 ℃ (other conditions are the same). The process conditions for directly carrying out hydroconversion on catalytic diesel without cutting treatment are generally as follows: the reaction pressure is 3.0-15.0 MPa, preferably 5.0-12.0 MPa; the liquid hourly space velocity is 0.1-15.0 h < -1 >, preferably 0.2-3.0 h < -1 >, and the average reaction temperature of the hydrofining reaction zone is 300-450 ℃, preferably 350-400 ℃.
The above process, the hydrocracking catalyst in step (3) generally comprises a cracking component, a hydrogenation component and a binder. The catalyst may be prepared using commercially available products or according to the prior art. The cracking component is Y-type molecular sieve. The binder is typically alumina or silica. The hydrogenation active metal component is a metal component of the VIB group and/or the VIII group, for example, one or more of Co, ni, mo, W. The content of the hydrogenation component is usually 3-20wt%, and the content of the cracking component is 30-80wt%, preferably 40-70wt%, based on the weight of the hydroconversion catalyst.
In the step (3) of the above method, the reaction conditions in the hydrocracking reaction zone are generally as follows: the reaction pressure is 3.0-15.0 MPa, preferably 5.0-12.0 MPa; the liquid hourly space velocity is 0.1 to 15.0h -1 Preferably 0.2 to 3.0h -1 The average reaction temperature of the hydroconversion reaction zone is 300-450 ℃, preferably380℃~420℃。
In the step (3) of the method, the aromatic hydrocarbon extraction can be performed by adopting the prior art, and the conventional aromatic hydrocarbon extraction method mainly comprises the following steps: liquid-liquid extraction or extractive distillation. The invention selects liquid-liquid extraction method, and the extraction solvent is one or more of di (triethylene) glycol, tetraethylene glycol, sulfolane, N-methylpyrrolidone and dimethyl sulfoxide. The extraction temperature is 20-200 ℃, preferably 50-150 ℃; solvent: the mass ratio of the heavy naphtha is 1:1-8:1, preferably 3:1-5:1; the pressure is 0MPa to 2MPa, preferably 0.1 to 0.5MPa.
Those skilled in the art generally recognize that as petroleum fractions become heavier, their nitrogen content gradually increases, which increases in a process similar to the distillation range profile in petroleum, is a slow increasing process. However, the inventor found through intensive research that the catalytic diesel oil also shows the increasing trend of nitrogen content along with the heavy distillation range, but the increasing process is gentler when the distillation range is lighter, and the nitrogen content is increased in multiple when the final distillation point reaches a certain temperature, further research shows that the hydrotreating is carried out after cutting out a part of the fraction with proper content, thereby obviously reducing the hydrotreating condition, reducing the aromatic saturation and improving the aromatic yield
Compared with the prior art, the hydrogenation method for producing BTX has the following advantages: the enrichment degree of tricyclic aromatic hydrocarbon and nitrogen in the catalytic diesel is high, the proportion of the heavy component content in the catalytic diesel is low, the operation severity of the catalytic diesel hydro-conversion device can be greatly reduced by removing the heavy component, particularly the reduction of the reaction pressure, and the aromatic hydrocarbon loss caused by the hydrogenation process can be effectively reduced.
Drawings
FIG. 1 is a schematic flow diagram of a hydrogenation process for producing BTX according to an embodiment of the present invention.
Wherein 1 is catalytic diesel, 2 is a fractionating tower, 3 is catalytic cracking diesel heavy fraction, 4 is catalytic cracking diesel light fraction, 5 is hydrogen, 6 is a hydrofining reaction zone, 7 is hydrofining reaction effluent, 8 is hydrocracking reaction zone, 9 is hydrocracking reaction effluent, 10 is a separator, 11 is a separated gas phase, 12 is a separated liquid phase, 13 is a fractionating tower, 14 is gas, 15 is light naphtha, 16 is heavy naphtha, 17 is tail oil, 18 is aromatic hydrocarbon extraction zone, 19 is BTX component, and 20 is raffinate oil.
Detailed Description
The operation and effect of the present invention will be further illustrated by the following examples, which are not to be construed as limiting the process of the present invention, and are all percentages by mass unless otherwise specified.
As shown in fig. 1, catalytic cracking diesel 1 enters a fractionating tower 2 to be separated to obtain a catalytic cracking diesel heavy fraction 3 and a catalytic cracking diesel light fraction 4, the catalytic cracking diesel light fraction 4 is mixed with hydrogen 5 to enter a hydrofining reaction zone 6, hydrofining reaction effluent 7 enters a hydrocracking reaction zone 8, hydrocracking reaction effluent 9 enters a separator 10, separated gas phase 11 is recycled, liquid phase 12 enters a fractionating tower 13 to be separated to obtain gas 14, light naphtha 15, heavy naphtha 16 and tail oil 17, the heavy naphtha 16 enters an aromatic hydrocarbon extraction zone 18, and BTX component 19 and raffinate oil 20 are separated.
The catalyst adopted in the hydrofining reaction zone in the embodiment of the invention is FF-66 hydrofining catalyst, the composition is MoO3 22wt%, niO 5 wt%, the rest is alumina, the catalyst adopted in the hydrocracking reaction zone is FC-70A hydrocracking catalyst, the composition is MoO3 12wt%, niO 3wt%, Y-type molecular sieve content 60wt%, and the rest is alumina, and manufacturers of the catalysts are China petrochemical catalyst Co.
In the embodiment and the comparative example, the process conditions of using sulfolane as the extraction solvent are as follows: the extraction temperature is 80 ℃; solvent: the mass ratio of the heavy naphtha is 4:1; the pressure was 0.3MPa.
Table 1 shows the catalytic diesel properties; table 2 shows the conditions and the reaction results of the examples; table 3 shows the conditions and the reaction results of the comparative examples.
TABLE 1
TABLE 2
Comparative example 1
The catalytic cracking diesel oil firstly enters a hydrofining reaction zone to carry out hydrogenation saturation reaction, the hydrofining reaction zone is filled with FF-66 hydrofining catalyst, the effluent of the hydrofining reaction zone enters a hydrocracking reaction zone to carry out hydrocracking reaction, and the hydrocracking reaction zone is filled with FC-70A hydrocracking catalyst.
TABLE 3 Table 3
From the above examples, it can be seen that the method of the present invention can effectively increase the BTX yield in the product and prolong the operation time of the device.
Claims (10)
1. A hydrogenation process for producing BTX, the process comprising the steps of:
(1) Cutting the catalytic cracking diesel oil to obtain light and heavy distillate oil, wherein the cutting point is 300-350 ℃;
(2) The light distillate oil obtained in the step (1) enters a hydrofining reaction zone to carry out hydrofining reaction under the action of a hydrofining catalyst;
(3) The reaction material after hydrofining in the step (2) enters a hydrocracking reaction zone to carry out hydrocracking reaction under the action of a hydrocracking catalyst;
(4) And (3) feeding the hydrocracking generated oil obtained in the step (3) into a separation system for gas-liquid separation, recycling the separated gas as supplementary hydrogen, further separating the liquid phase product to obtain light naphtha, heavy naphtha and tail oil, and extracting the heavy naphtha by aromatic hydrocarbon to obtain BTX.
2. The method according to claim 1, characterized in that: the cutting point is 310-330 ℃.
3. The method according to claim 1, characterized in that: the initial boiling point of the catalytic diesel oil in the step (1) is 60-220 ℃, preferably 170-210 ℃; density of 0.90g/cm -3 ~0.99 g/cm -3 The method comprises the steps of carrying out a first treatment on the surface of the The nitrogen content is 0.03-0.2 m%; the aromatic hydrocarbon content is 50-90 m%, preferably 65-85 m%.
4. The method according to claim 1, characterized in that: the weight content of tricyclic aromatic hydrocarbon in the light distillate oil obtained in the step (1) is 0.1% -5%; the nitrogen content is 100 mg/kg-500 mg/kg.
5. The method according to claim 4, wherein: the weight content of the tricyclic aromatic hydrocarbon in the light distillate oil obtained in the step (1) is 0.2% -4%, preferably 1% -3%; the nitrogen content is 200 mg/kg-300 mg/kg.
6. The method according to claim 1, characterized in that: the hydrofining catalyst in the step (2) contains a metal component of group VIB and/or group VIII, wherein the group VIB is selected from tungsten and/or molybdenum, the content of the group VIB in the catalyst is 5% -30% by weight of oxide substances, preferably 10% -20%, and the content of the group VIII in the catalyst is selected from nickel and/or cobalt, and the content of the group VIII in the catalyst is 1% -6% by weight of oxide substances, preferably 1.5% -5%.
7. The method according to claim 1, characterized in that: compared with the process conditions that catalytic diesel is directly subjected to hydroconversion without cutting treatment, the reaction conditions of the hydrofining reaction zone in the step (2) are as follows: the reaction pressure is lower by 0.5-6.0 MPa, preferably 1.0-3.0 MPa; the average temperature is 5-30 ℃, preferably 10-20 ℃.
8. The method according to claim 1, characterized in that: the technological conditions for directly carrying out hydroconversion on the catalytic diesel without cutting treatment are as follows: the reaction pressure is 3.0-15.0 MPa, preferably 5.0-12.0 MPa; the liquid hourly space velocity is 0.1-15.0 h < -1 >, preferably 0.2-3.0 h < -1 >, and the average reaction temperature of the hydrofining reaction zone is 300-450 ℃, preferably 350-400 ℃.
9. The method according to claim 1, characterized in that: the hydrocracking catalyst in step (3) generally comprises a cracking component, a hydrogenation component and a binder, wherein the cracking component is a Y-type molecular sieve, the binder is alumina or silica, and the hydrogenation active metal component is a group VIB and/or a group VIII metal component.
10. The method according to claim 1, characterized in that: in the step (3), the reaction conditions of the hydrocracking reaction zone are as follows: the reaction pressure is 3.0-15.0 MPa, preferably 5.0-12.0 MPa; the liquid hourly space velocity is 0.1 to 15.0h -1 Preferably 0.2 to 3.0h -1 The average reaction temperature of the hydroconversion reaction zone is 300-450 ℃, preferably 380-420 ℃.
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