CN108048133B - Method for joint production of n-hexane and clean gasoline blending component - Google Patents
Method for joint production of n-hexane and clean gasoline blending component Download PDFInfo
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- CN108048133B CN108048133B CN201711312768.2A CN201711312768A CN108048133B CN 108048133 B CN108048133 B CN 108048133B CN 201711312768 A CN201711312768 A CN 201711312768A CN 108048133 B CN108048133 B CN 108048133B
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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Abstract
The invention discloses a method for jointly producing n-hexane and clean gasoline blending components, which comprises the following steps: (1) adding the arene extraction by-product into a fiber membrane contactor, and performing desulfurization treatment; (2) dehydrating the desulfurized product; (3) carrying out hydrogenation treatment on the dehydrated product; (4) and rectifying and separating the product after the hydrotreatment to obtain the normal hexane and clean gasoline blending component. The method for jointly producing the n-hexane and the clean gasoline blending component reasonably utilizes the aromatic extraction by-product to the maximum extent, avoids the treatment of the product obtained after the n-hexane fraction is obtained in the conventional production process as solvent oil with lower added value, can obtain the low-sulfur and higher gasoline octane number blending component, can relieve the requirement pressure of clean gasoline at present, and is a novel process for preparing the n-hexane and the clean gasoline blending component by utilizing the aromatic extraction by-product with high added value.
Description
Technical Field
The invention relates to a method for producing n-hexane and clean gasoline blending components, in particular to a method for producing high-additive n-hexane and clean gasoline blending components by adopting a hydrogenation rectification process.
Background
Benzene, toluene and xylene are commonly called triphenyl in industry, are used as chemical raw materials or solvents and are widely applied to the industries of dye industry, agricultural production, spice manufacturing, pharmacy and the like. At present, the catalytic reforming technology is mainly adopted for production, but due to the technical limitation of the process, the yield of aromatic hydrocarbon, particularly benzene, of a catalytic reforming device is low, and a considerable part of by-product, namely aromatic hydrocarbon raffinate oil, accounts for about 30-40% of the reformed oil. The aromatic raffinate oil (the boiling range is less than or equal to 90 ℃) is mainly saturated hydrocarbon of C6-C8, the content of normal hexane is 20-30%, the content of total isomeric hydrocarbon is 65-75%, a small amount of olefin is contained, the content of aromatic hydrocarbon is low, and the content of sulfur, nitrogen and heavy metal impurities is extremely low. At present, the reformed aromatic raffinate oil is mainly used for producing various high-quality solvent oils and hexane oils with high added values; as the octane number (RON) of the aromatic raffinate oil is only 60-70, the aromatic raffinate oil is limited to be used as a gasoline blending component, and the aromatic raffinate oil is low in added value when being used as solvent oil.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide a method for jointly producing normal hexane and a clean gasoline blending component.
In order to achieve the purpose, the invention adopts the technical scheme that: a method for jointly producing n-hexane and a clean gasoline blending component comprises the following steps:
(1) adding the arene extraction by-product into a fiber membrane contactor, and performing desulfurization treatment;
(2) dehydrating the desulfurized product;
(3) carrying out hydrogenation treatment on the dehydrated product;
(4) and rectifying and separating the product after the hydrotreatment to obtain the normal hexane and clean gasoline blending component.
The aromatic extraction by-product is distillate oil obtained by extracting aromatic hydrocarbon from reformed oil rich in aromatic hydrocarbon C6-C8 in the petroleum refining process, and the main components of the distillate oil are C6-C8 saturated hydrocarbon and a small amount of olefin and aromatic hydrocarbon.
The method takes an aromatic extraction byproduct as a raw material, the raw material contains a small amount of sulfur, the sulfur content is 50-100 PPM, the raw material is mainly sulfolane (extraction solvent) carried in the aromatic extraction process, softened water is adopted to remove the sulfolane through water washing of a fiber membrane contactor by utilizing the characteristic that the sulfolane is mutually soluble with water, then water is removed, olefin and aromatic hydrocarbon are removed through hydrogenation reaction, a reaction product is rectified and separated to obtain n-hexane and clean gasoline blending components, and the content of the obtained n-hexane is more than or equal to 70%.
As a preferred embodiment of the method for jointly producing the normal hexane and the clean gasoline blending component, the method further comprises the following step (3) and before the step (4), and further comprises the following step (3 a): after the material is hydrotreated, the material enters a heat exchanger for cooling, and then the material passes through a gas-liquid separator to obtain a hydrotreated product.
As a preferred embodiment of the method for jointly producing the normal hexane and the clean gasoline blending component, in the step (1), the oil-water ratio of desulfurization treatment in the fiber membrane contactor is 10: 2-4.
If the oil-water ratio is too large, the power cost is high, and if the oil-water ratio is too small, the desulfurization effect is poor. Repeated experiments of the inventor show that the oil-water ratio can ensure the desulfurization effect and the desulfurization efficiency at the same time.
As a preferred embodiment of the method for jointly producing the normal hexane and the clean gasoline blending component, in the step (1), the operating temperature in the fiber membrane contactor is 35-45 ℃, the operating pressure is 0.1-0.25 MPa, and the pressure drop of the fiber membrane contactor is 0.06-0.08 MPa.
The sulphur content in the desulphurised product obtained under the operating conditions described above is less than 0.5 PPM.
As a preferred embodiment of the method for jointly producing the normal hexane and the clean gasoline blending component, in the step (2), the device adopted by the dehydration treatment is a molecular sieve dehydration tower.
As a preferred embodiment of the method for jointly producing the n-hexane and the clean gasoline blending component, the water content of the dehydrated product is less than or equal to 50 PPM.
As a preferred embodiment of the method for jointly producing n-hexane and clean gasoline blending components, in the step (3), the device adopted by the hydrogenation treatment is two hydrogenation reactors connected in series: hydrogenation reactor I and hydrogenation reactor II.
The hydrogenation reactor I is used for removing olefin; the hydrogenation reactor II is used for removing aromatic hydrocarbon.
As the preferred embodiment of the method for jointly producing the n-hexane and the clean gasoline blending component, the reaction pressure of the hydrogenation reactor I is 1.80-2.20 MPa, the reaction temperature is 155-165 ℃, and the space velocity is 2-4 h-1The volume ratio of the hydrogen to the dehydrated product is: hydrogen gas: and (3) the dehydrated product is 500-800: 1.
As the preferred embodiment of the method for jointly producing the n-hexane and the clean gasoline blending component, the reaction pressure of the hydrogenation reactor II is 1.80-2.00 MPa, the reaction temperature is 150-165 ℃, and the airspeed is 2-3 h-1The volume ratio of the hydrogen to the dehydrated product is: hydrogen gas: the dehydrated product is 300-500: 1.
In the present invention, the volume ratio of hydrogen gas to dehydrated product is referred to as the hydrogen-oil ratio. The energy consumption is increased due to the overlarge hydrogen-oil ratio, and the operation cost of the device is overhigh; too low a hydrogen-to-oil ratio may result in incomplete hydrogenation and affect product quality.
The hydrotreatment adopts two-stage hydrotreatment, the hydrotreatment is carried out under the conditions, the hydrogenation efficiency is high, the bromine index of the product after the hydrotreatment is not more than 5mgBr/100g, and the benzene content is less than 50 PPM.
As a preferred embodiment of the method for jointly producing the normal hexane and the clean gasoline blending component, in the step (4), the rectification separation adopts two rectification towers which are connected in series: a first rectifying column and a second rectifying column; the operating conditions of the first rectifying tower are as follows: the feeding temperature is 35-45 ℃, the top temperature is 62-66 ℃, the bottom temperature is 75-82 ℃, the top reflux temperature is 30-40 ℃, the top reflux ratio is 60-80, and the operating absolute pressure of the tower is 0.10-0.12 MPa; the operating conditions of the second rectification column are as follows: the feeding temperature is 70-80 ℃, the top temperature is 60-63 ℃, the bottom temperature is 79-85 ℃, the top reflux temperature is 30-40 ℃, the top reflux ratio is 50-70, and the absolute operating pressure of the tower is 0.10-0.12 MPa.
As a preferred embodiment of the method for co-producing n-hexane and clean gasoline blending components, the ratio of the height to the diameter of the first rectifying tower is 28:1, the ratio of the height to the diameter of the second rectifying tower is 30:1, the internal parts of the first rectifying tower and the second rectifying tower are matched by adopting a wire mesh and a corrugated packing of a structured packing layer, and the weight ratio of the wire mesh to the corrugated packing of the structured packing layer is as follows: silk screen of the structured packing layer: corrugated packing 1.5: 1.
Because the octane number (RON) of the reformed aromatic raffinate oil is only 60-70, the components of the reformed aromatic raffinate oil contain 20-30% of normal hexane, and the octane number (RON) of the normal hexane is only 25, the separation efficiency can be improved by adopting the wire mesh and the corrugated packing of the regular packing layer, the component (normal hexane) with the lower octane number is extracted from the raw materials to the maximum extent, the content of isoparaffin of the product is improved, and the octane number of the product is correspondingly improved.
The method has the advantages that: the invention provides a method for jointly producing normal hexane and clean gasoline blending components, which adopts different technological processes to be mutually combined and continuously produces high-quality normal hexane and high-quality gasoline blending components, and compared with the traditional aromatic raffinate oil treatment process, the obtained product has higher added value; the content of normal hexane is more than 70%, and the distillation range is narrow (66-70 ℃); the octane number (RON) of gasoline blending components is above 86, the benzene content is less than 50PPM, the sulfur content is not more than 0.5PPM, and the bromine index is not more than 5mgBr/100 g. The method for jointly producing the n-hexane and the clean gasoline blending component reasonably utilizes the aromatic extraction by-product to the maximum extent, avoids the treatment of the product obtained after the n-hexane fraction is obtained in the conventional production process as solvent oil with lower added value, can obtain the low-sulfur and higher gasoline octane number blending component, can relieve the requirement pressure of clean gasoline at present, and is a novel process for preparing the n-hexane and the clean gasoline blending component by utilizing the aromatic extraction by-product with high added value.
Detailed Description
Example 1
In an embodiment of the method for co-producing n-hexane and a clean gasoline blending component, the method for co-producing n-hexane and a clean gasoline blending component comprises the following steps:
(1) adding the aromatic extraction by-product into a fiber membrane contactor, and removing sulfolane carried by aromatic raffinate oil by washing, wherein the operating conditions are that the oil-water ratio is 10:4, the operating temperature is 40 ℃, the operating pressure is 0.25MPa, and the pressure drop of the fiber membrane contactor is 0.06 MPa;
(2) dehydrating the desulfurized product in a molecular sieve dehydration tower;
(3) sequentially feeding the dehydrated product into a hydrogenation reactor I and a hydrogenation reactor II for hydrogenation treatment, and carrying out olefin removal treatment on the hydrogenation reactor I, wherein the reaction pressure of the olefin removal reactor is 1.80MPa, and the reaction temperature is 155 ℃ and space velocity of 2h-1The hydrogen-oil ratio is 500: 1; the hydrogenation reactor II is subjected to dearomatization treatment, the reaction pressure of the dearomatization reactor is 1.80MPa, the reaction temperature is 160 ℃, and the space velocity is 2h-1The hydrogen-oil ratio is 300: 1; cooling by a heat exchanger, separating by a gas-liquid separator to obtain a hydrotreated product, and conveying hydrogen to a hydrogenation reactor for recycling;
(4) and the product after hydrotreating enters two rectifying towers connected in series: a first rectifying column and a second rectifying column; the height-diameter ratio of the first rectifying tower is 28:1, the height-diameter ratio of the second rectifying tower is 30:1, the tower internals of the first rectifying tower and the second rectifying tower adopt the matching of the silk screen of the regular packing layer and the corrugated packing, and the weight ratio of the silk screen of the regular packing layer to the corrugated packing is as follows: silk screen of the structured packing layer: 1.5:1 of corrugated filler; the operating conditions of the first rectification column are as follows: the feeding temperature is 36 ℃, the top temperature is 62 ℃, the bottom temperature is 78 ℃, the top reflux temperature is 35 ℃, the top reflux ratio is 60, and the operating absolute pressure of the tower is 0.10 MPa; the operating conditions of the second rectification column are as follows: the feeding temperature is 70 ℃, the top temperature is 60 ℃, the bottom temperature is 82 ℃, the top reflux temperature is 30 ℃, the top reflux ratio is 50, and the tower operating absolute pressure is 0.11 MPa. And n-hexane is separated from the top of the second rectifying tower, and the rest components are high-quality gasoline blending components to obtain the n-hexane and clean gasoline blending components.
Example 2
In an embodiment of the method for co-producing n-hexane and a clean gasoline blending component, the method for co-producing n-hexane and a clean gasoline blending component comprises the following steps:
(1) adding the aromatic extraction by-product into a fiber membrane contactor, and removing sulfolane carried by aromatic raffinate oil by washing, wherein the operating conditions are that the oil-water ratio is 10:2, the operating temperature is 35 ℃, the operating pressure is 0.20MPa, and the pressure drop of the fiber membrane contactor is 0.08 MPa;
(2) dehydrating the desulfurized product in a molecular sieve dehydration tower;
(3) and sequentially dehydrating the productThe mixture enters a hydrogenation reactor I and a hydrogenation reactor II for hydrogenation treatment, the hydrogenation reactor I carries out olefin removal treatment, the reaction pressure of the olefin removal reactor is 1.90MPa, the reaction temperature is 160 ℃, and the space velocity is 3h-1The hydrogen-oil ratio is 600: 1; the hydrogenation reactor II is subjected to dearomatization treatment, the reaction pressure of the dearomatization reactor is 1.90MPa, the reaction temperature is 155 ℃, and the airspeed is 2.5h-1The hydrogen-oil ratio is 400: 1; cooling by a heat exchanger, separating by a gas-liquid separator to obtain a hydrotreated product, and conveying hydrogen to a hydrogenation reactor for recycling;
(4) and the product after hydrotreating enters two rectifying towers connected in series: a first rectifying column and a second rectifying column; the height-diameter ratio of the first rectifying tower is 28:1, the height-diameter ratio of the second rectifying tower is 30:1, the tower internals of the first rectifying tower and the second rectifying tower adopt the matching of the silk screen of the regular packing layer and the corrugated packing, and the weight ratio of the silk screen of the regular packing layer to the corrugated packing is as follows: silk screen of the structured packing layer: 1.5:1 of corrugated filler; the operating conditions of the first rectifying tower are as follows: the feeding temperature is 38 ℃, the top temperature is 63 ℃, the bottom temperature is 80 ℃, the top reflux temperature is 40 ℃, the top reflux ratio is 70, and the tower operation absolute pressure is 0.11 MPa; the operating conditions of the second rectifying tower are as follows: the feed temperature was 72 ℃, the overhead temperature was 61 ℃, the bottom temperature was 83 ℃, the overhead reflux temperature was 35 ℃, the overhead reflux ratio was 60, and the column operating absolute pressure was 0.11 MPa. And n-hexane is separated from the top of the second rectifying tower, and the rest components are high-quality gasoline blending components to obtain the n-hexane and clean gasoline blending components.
Example 3
In an embodiment of the method for co-producing n-hexane and a clean gasoline blending component, the method for co-producing n-hexane and a clean gasoline blending component comprises the following steps:
(1) adding the aromatic extraction by-product into a fiber membrane contactor, and removing sulfolane carried by aromatic raffinate oil by washing, wherein the operating conditions are that the oil-water ratio is 10:3, the operating temperature is 40 ℃, the operating pressure is 0.22MPa, and the pressure drop of the fiber membrane contactor is 0.07 MPa;
(2) dehydrating the desulfurized product in a molecular sieve dehydration tower;
(3) sequentially feeding the dehydrated product into a hydrogenation reactor I and a hydrogenation reactor II for hydrogenation treatment, wherein the hydrogenation reactor I is subjected to olefin removal treatment, the reaction pressure of the olefin removal reactor is 2.10MPa, the reaction temperature is 160 ℃, and the airspeed is 4h-1The hydrogen-oil ratio is 700: 1; the hydrogenation reactor II is subjected to dearomatization treatment, the reaction pressure of the dearomatization reactor is 2.00MPa, the reaction temperature is 160 ℃, and the space velocity is 3h-1The hydrogen-oil ratio is 400: 1; cooling by a heat exchanger, separating by a gas-liquid separator to obtain a hydrotreated product, and conveying hydrogen to a hydrogenation reactor for recycling;
(4) and the product after hydrotreating enters two rectifying towers connected in series: a first rectifying column and a second rectifying column; the height-diameter ratio of the first rectifying tower is 28:1, the height-diameter ratio of the second rectifying tower is 30:1, the tower internals of the first rectifying tower and the second rectifying tower adopt the matching of the silk screen of the regular packing layer and the corrugated packing, and the weight ratio of the silk screen of the regular packing layer to the corrugated packing is as follows: silk screen of the structured packing layer: 1.5:1 of corrugated filler; the operating conditions of the first rectification column are as follows: the feeding temperature is 40 ℃, the top temperature is 64 ℃, the bottom temperature is 81 ℃, the top reflux temperature is 40 ℃, the top reflux ratio is 70, and the operating absolute pressure of the tower is 0.11 MPa; the operating conditions of the second rectification column are as follows: the feed temperature was 72 ℃, the overhead temperature was 62 ℃, the bottom temperature was 83 ℃, the overhead reflux temperature was 40 ℃, the overhead reflux ratio was 70, and the column operating absolute pressure was 0.11 MPa. And n-hexane is separated from the top of the second rectifying tower, and the rest components are high-quality gasoline blending components to obtain the n-hexane and clean gasoline blending components.
Example 4
In an embodiment of the method for co-producing n-hexane and a clean gasoline blending component, the method for co-producing n-hexane and a clean gasoline blending component comprises the following steps:
(1) adding the aromatic extraction by-product into a fiber membrane contactor, and removing sulfolane carried by aromatic raffinate oil by washing, wherein the operating conditions are that the oil-water ratio is 10:3, the operating temperature is 45 ℃, the operating pressure is 0.1MPa, and the pressure drop of the fiber membrane contactor is 0.07 MPa;
(2) dehydrating the desulfurized product in a molecular sieve dehydration tower;
(3) sequentially feeding the dehydrated product into a hydrogenation reactor I and a hydrogenation reactor II for hydrogenation treatment, wherein the hydrogenation reactor I is subjected to olefin removal treatment, the reaction pressure of the olefin removal reactor is 2.20MPa, the reaction temperature is 160 ℃, and the airspeed is 4h-1The hydrogen-oil ratio is 800: 1; the hydrogenation reactor II is subjected to dearomatization treatment, the reaction pressure of the dearomatization reactor is 2.00MPa, the reaction temperature is 160 ℃, and the space velocity is 3h-1The hydrogen-oil ratio is 500: 1; cooling by a heat exchanger, separating by a gas-liquid separator to obtain a hydrotreated product, and conveying hydrogen to a hydrogenation reactor for recycling;
(4) and the product after hydrotreating enters two rectifying towers connected in series: a first rectifying column and a second rectifying column; the height-diameter ratio of the first rectifying tower is 28:1, the height-diameter ratio of the second rectifying tower is 30:1, the tower internals of the first rectifying tower and the second rectifying tower adopt the matching of the silk screen of the regular packing layer and the corrugated packing, and the weight ratio of the silk screen of the regular packing layer to the corrugated packing is as follows: silk screen of the structured packing layer: 1.5:1 of corrugated filler; the operating conditions of the first rectification column are as follows: the feeding temperature is 45 ℃, the top temperature is 65 ℃, the bottom temperature is 82 ℃, the top reflux temperature is 40 ℃, the top reflux ratio is 80, and the operating absolute pressure of the tower is 0.12 MPa; the operating conditions of the second rectification column are as follows: the feed temperature was 75 ℃, the overhead temperature was 63 ℃, the bottom temperature was 84 ℃, the overhead reflux temperature was 35 ℃, the overhead reflux ratio was 70, and the column operating absolute pressure was 0.12 MPa. And n-hexane is separated from the top of the second rectifying tower, and the rest components are high-quality gasoline blending components to obtain the n-hexane and clean gasoline blending components.
Example 5
The n-hexane and clean gasoline blending components prepared in the embodiments 1 to 4 are subjected to relevant test analysis, and test results are shown in tables 1 and 2.
TABLE 1 analysis of n-Hexane results
TABLE 2 clean gasoline blending component results analysis
As can be seen from tables 1 and 2, the method for jointly producing the normal hexane and the clean gasoline blending component can maximally and reasonably utilize the aromatic raffinate oil to produce the normal hexane with high added value and the clean gasoline blending component with high quality.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the protection scope of the present invention, and although the present invention is described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions can be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.
Claims (6)
1. A method for jointly producing n-hexane and a clean gasoline blending component is characterized by comprising the following steps:
(1) adding the arene extraction by-product into a fiber membrane contactor, and performing desulfurization treatment;
(2) dehydrating the desulfurized product;
(3) carrying out hydrogenation treatment on the dehydrated product;
(4) rectifying and separating the product after the hydrotreatment to obtain the normal hexane and clean gasoline blending component;
in the step (3), the hydrogenation device comprises two hydrogenation reactors connected in series: a hydrogenation reactor I and a hydrogenation reactor II; the reaction pressure of the hydrogenation reactor I1.80-2.20 MPa, reaction temperature of 155-165 ℃ and airspeed of 2-4 h-1The volume ratio of the hydrogen to the dehydrated product is: hydrogen gas: the dehydrated product is 500-800: 1; the reaction pressure of the hydrogenation reactor II is 1.80-2.00 MPa, the reaction temperature is 150-165 ℃, and the airspeed is 2-3 h-1The volume ratio of the hydrogen to the dehydrated product is: hydrogen gas: the dehydrated product is 300-500: 1;
in the step (4), the devices adopted for rectification separation are two rectification towers connected in series: a first rectifying column and a second rectifying column; the operating conditions of the first rectifying tower are as follows: the feeding temperature is 35-45 ℃, the top temperature is 62-66 ℃, the bottom temperature is 75-82 ℃, the top reflux temperature is 30-40 ℃, the top reflux ratio is 60-80, and the operating absolute pressure of the tower is 0.10-0.12 MPa; the operating conditions of the second rectification column are as follows: the feeding temperature is 70-80 ℃, the top temperature is 60-63 ℃, the bottom temperature is 79-85 ℃, the top reflux temperature is 30-40 ℃, the top reflux ratio is 50-70, and the absolute operating pressure of the tower is 0.10-0.12 MPa.
2. The method for jointly producing n-hexane and clean gasoline blending components according to claim 1, wherein in the step (1), the oil-water ratio of desulfurization treatment in the fiber membrane contactor is 10: 2-4.
3. The method for co-producing n-hexane and clean gasoline blending components according to claim 1, wherein in the step (1), the operating temperature in the fiber membrane contactor is 35-45 ℃, the operating pressure is 0.1-0.25 MPa, and the pressure drop of the fiber membrane contactor is 0.06-0.08 MPa.
4. The method for co-producing n-hexane and clean gasoline blending components according to claim 1, wherein in the step (2), the device used for dehydration is a molecular sieve dehydration tower.
5. The method of co-producing n-hexane and clean gasoline blending components of claim 1, wherein the moisture content of the dehydrated product is less than or equal to 50 PPM.
6. The method for co-producing n-hexane and clean gasoline blending components of claim 1, wherein the ratio of the height to the diameter of the first rectification column is 28:1, the ratio of the height to the diameter of the second rectification column is 30: 1; the tower internals of the first rectifying tower and the second rectifying tower are matched by adopting a silk screen and corrugated packing of a regular packing layer, and the weight ratio of the silk screen to the corrugated packing of the regular packing layer is as follows: silk screen of the structured packing layer: corrugated packing 1.5: 1.
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