CN113185996A - Multi-stage cross flow extraction device and method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid - Google Patents
Multi-stage cross flow extraction device and method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/27—Organic compounds not provided for in a single one of groups C10G21/14 - C10G21/26
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/307—Cetane number, cetane index
Abstract
A multi-stage cross flow extraction device and a method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid belong to the technical field of chemical separation and purification. The solvent multistage cross-flow extraction method adopts an extracting agent based on ionic liquid to realize the high-efficiency separation of the catalytic diesel oil polycyclic aromatic hydrocarbon mixture. The method comprises the steps that catalytic diesel aromatic hydrocarbon to be separated enters a first-stage extractor (C1) from the bottom, an extracting agent A1 enters the first-stage extractor (C1) from the top, and the top of the first-stage extractor (C1) is connected with the bottom of a second-stage extractor (C2); the extractant A2 enters a second-stage extractor (C2) from the top, and the bottoms of the first-stage extractor (C1) and the second-stage extractor (C2) are connected with the middle part of an extract flash tank (S2) for flash separation; the stream at the top of the second stage extractor (C2) was connected to the middle of the raffinate flash drum (S1) for flash separation. The method overcomes the problem of mixing and dissolving the solvent and the raw materials, improves the yield of the oil product, ensures high purity of the separated oil product, and obtains the diesel component with high cetane number and the aromatic hydrocarbon with low alkane content.
Description
Technical Field
The invention relates to a multi-stage cross flow extraction device and method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid. The ionic liquid extractant can be single ionic liquid, mixed ionic liquid, a mixture of the ionic liquid and a traditional organic solvent or functional ionic liquid. Belongs to the technical field of chemical separation and purification.
Background
Under the great trend of developing low-carbon circular economy and realizing sustainable development of the environment, the upgrading pace of the diesel oil quality is obviously accelerated, and especially the limits on the cetane number and the polycyclic aromatic hydrocarbon index are more and more strict. The crude oil in China is mostly heavy and lacks for producing light raw materials of aromatic hydrocarbon and olefin. Catalytic cracking is an important means for heavy oil conversion, has the advantages of strong raw material adaptability, high conversion rate, low cost and the like, and occupies a great position in the petroleum refining process. The process is characterized in that the paraffin and the cyclane in the feed are cracked, and the aromatic hydrocarbon has no damage capability basically. Therefore, catalytic diesel is usually enriched with a large amount of polycyclic aromatic hydrocarbons, and this disadvantage is more prominent when the residual oil content in the raw material is large. At present, the technology of FCC diesel oil hydro-upgrading in China is rapidly developed under the limitation of environmental protection requirements and the promotion of market demands, but the hydro-upgrading process has high operation cost and harsh operation conditions, so that the production cost of diesel oil is greatly increased. The solvent extraction technology can effectively separate non-aromatic hydrocarbon and aromatic hydrocarbon, and the process can be applied to various material flows in an oil refinery: gasoline, kerosene, diesel and heavy distillates. At present, various solvents are applied to an industrial device for extracting aromatic hydrocarbon worldwide, and triethylene glycol, tetraethylene glycol, sulfolane, dimethyl sulfoxide, N-methylpyrrolidone, N-formylmorpholine and the like are common (common extraction solvents are shown in Table 1). However, these solvents are not suitable for catalytic diesel aromatics extraction because their boiling point is within the distillation range of catalytic diesel (180-; on the other hand, although the boiling point of the solvent such as furfural and N, N-Dimethylformamide (DMF) used for the extraction of lubricating oil is not within the distillation range of catalytic diesel oil, the solvent cannot be recovered by a conventional distillation method because it forms an azeotrope with many components in catalytic diesel oil. The ionic liquid is used as a novel separating agent for catalyzing the extraction of the diesel polycyclic aromatic hydrocarbon instead of a conventional solvent which is difficult to recycle, a novel functional ionic liquid polycyclic aromatic hydrocarbon extraction technology is creatively provided, the application range of the ionic liquid in chemical separation is widened, and the extraction process of the polycyclic aromatic hydrocarbon is strengthened. Therefore, how to economically and efficiently treat and catalyze poor diesel oil, improve the cetane number and reduce the content of polycyclic aromatic hydrocarbon becomes an important technical challenge facing the construction of catalytic device enterprises.
Chinese patent CN102021024A discloses a system and method for preparing high quality diesel oil, the system includes an extraction device, a part of aromatic hydrocarbons in diesel oil are removed by solvent extraction, high quality diesel oil is obtained by hydrogenation treatment of raffinate oil, and the extracted aromatic hydrocarbons are discharged from the system. The raw materials processed by the method are diversified, can be various diesel oil, and the aromatic hydrocarbon is separated from the diesel oil, so that the cetane number of the diesel oil is greatly improved, and the condensation point of the diesel oil is reduced.
Chinese patent CN102443436A discloses a combined method of residual oil hydrotreating, catalysis and diesel oil aromatic extraction. In the method, residual oil is hydrotreated in the presence of hydrogen and a hydrogenation catalyst, effluent is separated to obtain a gas-phase product and a liquid-phase product, the liquid-phase product directly enters a catalytic device for reaction without fractionation, the reaction effluent is separated to obtain dry gas, liquefied gas, catalytic gasoline, catalytic diesel and heavy distillate oil, the catalytic diesel is extracted by aromatic hydrocarbon, extract oil and the catalytic heavy distillate oil are recycled to the hydrotreating device after being filtered, and raffinate oil is discharged from the device to obtain the diesel with high cetane number. In the method, the hydrocracking reaction effluent is directly fed into the catalytic device for reaction without fractionation, so that the load of the catalytic device is increased undoubtedly, and the processing capacity of the device is influenced; secondly, the effluent of the hydrocracking reaction contains a certain amount of light components, and the light components enter a catalytic device and then undergo secondary reaction, so that light distillate oil is reduced, the gas yield is increased, and certain economic loss is caused.
TABLE 1 Main physical Properties of conventional extractants
The invention realizes the high-efficiency separation of the catalytic diesel oil aromatic hydrocarbon mixture by a solvent extraction method and adopting an extracting agent based on the ionic liquid, reduces the energy consumption of the device and simultaneously reduces the equipment cost.
Disclosure of Invention
The invention aims to provide a device and a method for catalyzing diesel polycyclic aromatic hydrocarbon multistage cross flow extraction by using ionic liquid. The technology can reduce the solvent ratio, simultaneously overcome the problem of mixing and dissolving of the solvent and the mixture to be separated, simultaneously improve the separation efficiency of the aromatic hydrocarbon of the diesel oil and improve the quality of the diesel oil product with cetane number.
The invention is realized by the following technical scheme.
A multi-stage cross flow extraction device for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid is characterized in that,
comprises a first-stage extractor (or a mixer settler) (C1), a second-stage extractor (or a mixer settler) (C2), a raffinate flash tank (S1) and an extract flash tank (S2);
wherein the catalytic diesel aromatic hydrocarbon (F) to be separated enters a first-stage extractor (C1) from the bottom, a first extractant (A1) enters the first-stage extractor (C1) from a top extractant feeding hole, and a top produced liquid (L1) of the first-stage extractor (C1) is connected with the bottom of a second-stage extractor (C2); the second extractant (A2) enters the second-stage extractor (C2) from the top; the produced liquid (L2) at the top of the second-stage extractor (C2) is connected with the middle part of the extract flash tank (S1);
an extract (R1) rich in ionic liquid at the bottom of the first-stage extractor (C1) and an extract (R2) rich in ionic liquid at the bottom of the second-stage extractor (C2) are respectively connected to the middle part of an extract flash tank (S2);
the extractant (IL1) flowing out of the bottom of the raffinate flash tank (S1) and the extractant (IL2) flowing out of the bottom of the extract flash tank (S2) are connected with the feeding port of the extractant of the first-stage extractor (C1) for cyclic utilization; non-aromatic hydrocarbons in the catalytic diesel oil are obtained from the top of the raffinate flash tank (S1), and polycyclic aromatic hydrocarbons in the catalytic diesel oil are obtained from the top of the extract flash tank (S2).
The first extractant (A1) and the second extractant (A2) are the same or different and are ionic liquid extractants, and the ionic liquid extractants can be single ionic liquid, mixed ionic liquid, a mixture of the ionic liquid and a traditional organic solvent or functional ionic liquid. The cation of the common ionic liquid in the ionic liquid is imidazole, pyridine and the like, and the anion is [ BF4]]-,[PF6]-And [ NTf2]-And the like. The ionic liquid is functionalizedThe functional groups of the subpiquids mainly include hydroxyl, aryl, amine, cyano, and the like. The organic solvent in the mixed ionic liquid mainly comprises sulfolane, dimethyl sulfoxide, N-methyl pyrrolidone, N-formyl morpholine, dimethylformamide, NFM, phenol, furfural and the like.
The method for separating and catalyzing the diesel aromatic hydrocarbon by adopting the device to carry out multistage cross-flow extraction mainly comprises the following steps:
(1) a first extractant, namely an ionic liquid extractant (A1), enters a first-stage extractor (C1) from the top, catalytic diesel aromatic hydrocarbon to be separated enters the first-stage extractor (C1) from the bottom, and is subjected to countercurrent high-efficiency separation, an extract rich in ionic liquid is discharged from the bottom of the first-stage extractor (C1) and enters an extract flash tank (S2), and a raffinate rich in non-aromatic hydrocarbon is extracted from the top of the first-stage extractor (C1) and enters the bottom of a second-stage extractor (C2);
(2) a second extractant, namely an ionic liquid extractant (A2), enters a second-stage extractor (C2) from the top, an extract rich in ionic liquid at the bottom of the second-stage extractor (C2) enters the middle part of an extract flash tank (S2), high-efficiency separation is carried out, aromatic hydrocarbon (including polycyclic aromatic hydrocarbon) is obtained at the top of the extract flash tank (S2), the ionic liquid extractant is obtained at the bottom of the flash tank, a produced liquid at the top of the second-stage extractor (C2) enters the middle part of a raffinate flash tank (S1), high-efficiency separation is carried out, non-aromatic hydrocarbon (alkane, olefin and the like) is obtained at the top of the raffinate flash tank (S1), and the extractant ionic liquid is obtained at the bottom of the flash tank; ,
(3) the ionic liquid extractant stream outlets at the bottoms of the raffinate flash tank (S1) and the extract flash tank (S2) are connected with the extractant circulating stream at the extractant feed inlet of the first-stage extractor (C1).
According to another preferred embodiment of the present invention, it is characterized in that the operating pressure of the first stage extractor (C1) is 1 to 5atm, the operating temperature is 20 to 100 ℃, preferably 20 to 50 ℃, the feeding position of the catalytic diesel aromatic hydrocarbon in the first stage extractor (C1) is the bottom, and the feeding position of the extractant is the top;
the operating pressure of the second-stage extractor (C2) is 1-5 atm, the operating temperature is 20-100 ℃, preferably 20-50 ℃, the produced liquid at the top of the first-stage extractor (C1) is at the bottom of the feeding position of the second-stage extractor (C2), and the feeding position of the extractant is at the top;
according to another preferred embodiment of the present invention, it is characterized in that the operating pressure of the raffinate flash tank (S1) and the extract flash tank (S2) is 0.1 to 0.5atm, and the operating temperature is 50 to 150 ℃.
According to another preferred embodiment of the invention, it is characterized in that said catalytic aromatic hydrocarbon mixture can be mixed in any ratio.
According to another preferred embodiment of the invention, it is characterized in that the extractant is a single ionic liquid, a mixed ionic liquid or a mixture of an ionic liquid and a conventional organic solvent.
According to another preferred embodiment of the invention, the ratio of the total amount of extractant in each stage to the volume of catalytic diesel aromatics to be separated is 0.5 to 3: 1.
According to another preferred embodiment of the invention, when the mass ratio of the n-hexadecane to the 1-methylnaphthalene in the diesel aromatic hydrocarbon is (7-9) to (1-3), the recovery rate of the separated n-hexadecane is 98.50-99.99%, and the recovery rate of the 1-methylnaphthalene is 96-99.9%.
Compared with the prior art, the invention mainly has the following beneficial effects:
(1) the method has simple process and convenient operation, successfully separates the catalytic diesel oil aromatic hydrocarbon mixture, improves the cetane number of the diesel oil product, and reduces the polycyclic aromatic hydrocarbon content in the oil product.
(2) The method adopts the extracting agent based on the ionic liquid, strengthens the separation effect of the extraction process, has simple extracting agent recovery process, reduces the energy consumption of the process and further reduces the process cost.
Drawings
FIG. 1 is a process flow diagram of multi-stage cross-flow extraction of diesel polycyclic aromatic hydrocarbons catalyzed by ionic liquid.
In the figure, C1 — first stage extractor (or mixer settler); c2-second stage extractor (or mixer settler); s1-raffinate flash tank; s2-extract liquid flash tank; f-to-be-separated catalytic diesel aromatic hydrocarbon, A1-a first extracting agent, A2-a second extracting agent, L1-a produced liquid at the top of a first-stage extractor, L2-a produced liquid at the top of a second-stage extractor, R1-an extract liquid rich in ionic liquid at the bottom of the first-stage extractor, R2-an extract liquid rich in ionic liquid at the bottom of the second-stage extractor, IL 1-an extracting agent flowing out from a flash tank of raffinate-a bottom of the flash tank, and IL 2-an extracting agent flowing out from the bottom of the flash tank of the extract liquid.
Detailed Description
The present invention will be further described with reference to examples, but the present invention is not limited to the following examples, and various examples are included in the technical scope of the present invention without departing from the spirit of the invention described above.
In the following examples, the first stage extractor (C1) and the second stage extractor (C2) were operated at normal temperature and pressure. The raffinate flash drum (S1) and extract flash drum (S2) were operated at 0.5atm and 100 deg.C.
Example 1:
common ionic liquid (specifically BMIM) (BF 4) is adopted as an extracting agent.
The feed flow is 100kg/h, and the feed contains 70 percent of n-hexadecane (mass fraction) and 30 percent of 1-methylnaphthalene (mass fraction). The feed position of the diesel fused ring aromatic hydrocarbon mixture is the bottom of a first-stage extractor (C1), the feed position of common ionic liquid is the top of the first-stage extractor (C1), produced liquid at the top of the first-stage extractor (C1) enters a second-stage extractor (C2) from the bottom, the common ionic liquid enters the second-stage extractor (C2) from the top, the volume ratio of the common ionic liquid to the feed of diesel aromatic hydrocarbon to be separated in each stage of extraction is 1:1, the recovery rate of n-hexadecane is 99.50% after multi-stage separation, and the recovery rate of 1-methylnaphthalene is 98.90%. The purity of n-hexadecane in the top extract of S1 was 99.8% (mass fraction), and the purity of 1-methylnaphthalene in the top raffinate of S2 was 98.5% (mass fraction).
Example 2:
mixed ionic liquid (specifically [ BMIM ] [ BF4] and [ EMIM ] [ BF4] in a volume ratio of 1:1) is adopted as an extracting agent.
The feed flow is 100kg/h, and the feed contains 80 percent (mass fraction) of n-hexadecane and 20 percent (mass fraction) of 1-methylnaphthalene. The feeding position of the diesel oil aromatic hydrocarbon mixture is the bottom of a first-stage extractor (C1), the feeding position of the mixed ionic liquid is the top of the first-stage extractor (C1), the produced liquid at the top of the first-stage extractor (C1) enters a second-stage extractor (C2) from the bottom, the ionic liquid enters the second-stage extractor (C2) from the top, the volume ratio of the ionic liquid to the feed of the diesel oil aromatic hydrocarbon to be separated in each stage of extraction is 1:1, the recovery rate of n-hexadecane is 99.60 percent after multi-stage separation, and the recovery rate of 1-methylnaphthalene is 99.10 percent. The purity of n-hexadecane in the top extract of S1 was 99.8% (mass fraction), and the purity of 1-methylnaphthalene in the top raffinate of S2 was 98.7% (mass fraction).
Example 3:
a mixed solution of common ionic liquid (specifically [ BMIM ] [ BF4]) + organic solvent (specifically sulfolane) (the volume ratio of the ionic liquid to the organic solvent is 3:7) is adopted as an extracting agent.
The feed flow rate was 100kg/h, and the feed contained 75 mass% of n-hexadecane and 25 mass% of 1-methylnaphthalene. The feeding position of the diesel oil aromatic hydrocarbon mixture is the bottom of a first-stage extractor (C1), the feeding position of the mixed extracting agent is the top of the first-stage extractor (C1), the produced liquid at the top of the first-stage extractor (C1) enters a second-stage extractor (C2) from the bottom, the mixed extracting agent enters the second-stage extractor (C2) from the top, the volume ratio of the mixed extracting agent to the diesel oil aromatic hydrocarbon to-be-separated material in each stage of extraction is 2:1, the recovery rate of the n-hexadecane is 99.8% after multi-stage separation, and the recovery rate of the 1-methylnaphthalene is 99.2%. The purity of n-hexadecane in the top extract of S1 was 99.8% (mass fraction), and the purity of 1-methylnaphthalene in the top raffinate of S2 was 98.9% (mass fraction).
Example 4:
hydroxyl functionalized ionic liquid (particularly HOCMIM ] [ PF 6) is adopted as an extracting agent.
The feed flow rate was 100kg/h, and the feed contained 75 mass% of n-hexadecane and 25 mass% of 1-methylnaphthalene. The feeding position of the diesel oil aromatic hydrocarbon mixture is the bottom of a first-stage extractor (C1), the feeding position of the hydroxyl functionalized ionic liquid is the top of the first-stage extractor (C1), the produced liquid at the top of the first-stage extractor (C1) enters a second-stage extractor (C2) from the bottom, the hydroxyl functionalized ionic liquid enters the second-stage extractor (C2) from the top, the volume ratio of the hydroxyl functionalized ionic liquid to the diesel oil aromatic hydrocarbon to-be-separated material in each stage of extraction is 2:1, the recovery rate of the n-hexadecane is 99.9 percent after multi-stage separation, and the recovery rate of the 1-methylnaphthalene is 99.5 percent. The purity of n-hexadecane in the top extract of S1 was 99.9% (mass fraction), and the purity of 1-methylnaphthalene in the top raffinate of S2 was 99.6% (mass fraction).
Example 5:
amino functionalized ionic liquid (specifically [ HNC2MIM ] [ PF6]) is used as an extracting agent.
The feed flow rate was 100kg/h, and the feed contained 75 mass% of n-hexadecane and 25 mass% of 1-methylnaphthalene. The feeding position of the diesel oil aromatic hydrocarbon mixture is the bottom of a first-stage extractor (C1), the feeding position of the amino functionalized ionic liquid is the top of the first-stage extractor (C1), the produced liquid at the top of the first-stage extractor (C1) enters a second-stage extractor (C2) from the bottom, the amino functionalized ionic liquid enters the second-stage extractor (C2) from the top, the volume ratio of the amino functionalized ionic liquid to the diesel oil aromatic hydrocarbon to-be-separated material in each stage of extraction is 2:1, the recovery rate of the n-hexadecane is 99.9 percent after multi-stage separation, and the recovery rate of the 1-methylnaphthalene is 99.4 percent. The purity of n-hexadecane in the top extract of S1 was 99.9% (mass fraction), and the purity of 1-methylnaphthalene in the top raffinate of S2 was 99.3% (mass fraction).
Example 6:
aryl functionalized ionic liquid (particularly BuPhIm BF 4) is adopted as an extracting agent.
The feed flow rate was 100kg/h, and the feed contained 75 mass% of n-hexadecane and 25 mass% of 1-methylnaphthalene. The feeding position of the diesel oil aromatic hydrocarbon mixture is the bottom of a first-stage extractor (C1), the feeding position of the choline base functionalized ionic liquid is the top of the first-stage extractor (C1), the produced liquid at the top of the first-stage extractor (C1) enters a second-stage extractor (C2) from the bottom, the choline base functionalized ionic liquid enters the second-stage extractor (C2) from the top, the volume ratio of the choline base functionalized ionic liquid to the diesel oil aromatic hydrocarbon to-be-separated substance feeding in each stage of extraction is 2:1, the recovery rate of the n-hexadecane is 99.9% after multi-stage separation, and the recovery rate of the 1-methylnaphthalene is 99.45%. The purity of n-hexadecane in the top extract of S1 was 99.9% (mass fraction), and the purity of 1-methylnaphthalene in the top raffinate of S2 was 99.4% (mass fraction).
The data show that the product separated by the method has high purity and high recovery rate, and the cetane number of the diesel oil product is greatly improved. The obtained high-purity aromatic hydrocarbon can be used for downstream production.
Claims (8)
1. A multi-stage cross flow extraction device for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid is characterized in that,
comprises a first-stage extractor (C1), a second-stage extractor (C2), a raffinate flash tank (S1) and an extract flash tank (S2);
wherein the catalytic diesel aromatic hydrocarbon (F) to be separated enters a first-stage extractor (C1) from the bottom, a first extractant (A1) enters the first-stage extractor (C1) from a top extractant feeding hole, and a top produced liquid (L1) of the first-stage extractor (C1) is connected with the bottom of a second-stage extractor (C2); the second extractant (A2) enters the second-stage extractor (C2) from the top; the produced liquid (L2) at the top of the second-stage extractor (C2) is connected with the middle part of the extract flash tank (S1);
an extract (R1) rich in ionic liquid at the bottom of the first-stage extractor (C1) and an extract (R2) rich in ionic liquid at the bottom of the second-stage extractor (C2) are respectively connected to the middle part of an extract flash tank (S2);
the extractant (IL1) flowing out of the bottom of the raffinate flash tank (S1) and the extractant (IL2) flowing out of the bottom of the extract flash tank (S2) are connected with the feeding port of the extractant of the first-stage extractor (C1) for cyclic utilization; non-aromatic hydrocarbons in the catalytic diesel oil are obtained from the top of the raffinate flash tank (S1), and polycyclic aromatic hydrocarbons in the catalytic diesel oil are obtained from the top of the extract flash tank (S2).
2. The multistage cross-flow extraction device for the catalytic diesel polycyclic aromatic hydrocarbon with the ionic liquid as claimed in claim 1, wherein the first extractant (A1) and the second extractant (A2) are the same or different and are ionic liquid extractants, and the ionic liquid extractants can be single ionic liquids, mixed ionic liquids, mixtures of ionic liquids and traditional organic solvents or functional ionic liquids.
3. The method for separating and catalyzing diesel aromatic hydrocarbon by adopting the device of claim 1 or 2 through multistage cross-flow extraction is characterized by mainly comprising the following steps:
(1) a first extractant, namely an ionic liquid extractant (A1), enters a first-stage extractor (C1) from the top, catalytic diesel aromatic hydrocarbon to be separated enters the first-stage extractor (C1) from the bottom, and is subjected to countercurrent high-efficiency separation, an extract rich in ionic liquid is discharged from the bottom of the first-stage extractor (C1) and enters an extract flash tank (S2), and a raffinate rich in non-aromatic hydrocarbon is extracted from the top of the first-stage extractor (C1) and enters the bottom of a second-stage extractor (C2);
(2) a second extractant, namely an ionic liquid extractant (A2), enters a second-stage extractor (C2) from the top, an extract rich in ionic liquid at the bottom of the second-stage extractor (C2) enters the middle part of an extract flash tank (S2), high-efficiency separation is carried out, aromatic hydrocarbon (including polycyclic aromatic hydrocarbon) is obtained at the top of the extract flash tank (S2), the ionic liquid extractant is obtained at the bottom of the flash tank, a produced liquid at the top of the second-stage extractor (C2) enters the middle part of a raffinate flash tank (S1), high-efficiency separation is carried out, non-aromatic hydrocarbon (alkane, olefin and the like) is obtained at the top of the raffinate flash tank (S1), and the extractant ionic liquid is obtained at the bottom of the flash tank; ,
(3) the ionic liquid extractant stream outlets at the bottoms of the raffinate flash tank (S1) and the extract flash tank (S2) are connected with the extractant circulating stream at the extractant feed inlet of the first-stage extractor (C1).
4. The process according to claim 3, characterized in that the first stage extractor (C1) is operated at a pressure of 1 to 5atm, at a temperature of 20 ℃ to 100 ℃, preferably 20 ℃ to 50 ℃, with the catalytic diesel aromatics at the bottom and the extractant at the top of the first stage extractor (C1).
5. The process according to claim 3, characterized in that the second stage extractor (C2) is operated at a pressure of 1 to 5atm, at a temperature of 20 ℃ to 100 ℃, preferably 20 ℃ to 50 ℃, the liquid output at the top of the first stage extractor (C1) being at the bottom at the feed position of the second stage extractor (C2) and the extractant feed position being at the top.
6. The process according to claim 3, characterized in that the raffinate flash tank (S1) and the extract flash tank (S2) are operated at an operating pressure of 0.1 to 0.5atm and an operating temperature of 50 to 150 ℃.
7. A process according to claim 3, characterized in that the ratio of the total amount of extractant in each extractor to the volume of catalytic diesel aromatics to be separated is 0.5 to 3: 1.
8. The method according to claim 3, wherein when the mass ratio of n-hexadecane to 1-methylnaphthalene in the diesel aromatic hydrocarbon is (7-9) to (1-3), the recovery rate of n-hexadecane after separation is 98.50-99.99%, and the recovery rate of 1-methylnaphthalene is 96-99.9%.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114849278A (en) * | 2022-04-20 | 2022-08-05 | 山东省产品质量检验研究院 | Multi-stage extractor for separating saturated hydrocarbon and unsaturated hydrocarbon in oil product |
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