CN108048133A - A kind of method of Joint Production n-hexane and clean gasoline blend component - Google Patents
A kind of method of Joint Production n-hexane and clean gasoline blend component Download PDFInfo
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- CN108048133A CN108048133A CN201711312768.2A CN201711312768A CN108048133A CN 108048133 A CN108048133 A CN 108048133A CN 201711312768 A CN201711312768 A CN 201711312768A CN 108048133 A CN108048133 A CN 108048133A
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- hexane
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- blend component
- gasoline blend
- clean gasoline
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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
-
- 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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- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of methods of Joint Production n-hexane and clean gasoline blend component, the described method comprises the following steps：(1), Aromatics Extractive Project by-product is added in fiber-film contact, desulfurization process；(2), the product after desulfurization process is carried out dehydrating；(3), the product after dehydration is subjected to hydrotreating；(4), the product after hydrotreating is subjected to rectifying separation, obtains the n-hexane and clean gasoline blend component.The method of Joint Production n-hexane and clean gasoline blend component of the present invention farthest rationally make use of Aromatics Extractive Project by-product, the solvent oil processing for avoiding the product in conventional production practices after acquisition hexane-fraction relatively low as added value, low-sulfur, higher octane number blend component can be obtained, it can alleviate now to the demand pressure of clean gasoline, be a kind of high value added utilization Aromatics Extractive Project by-product to prepare the new process of n-hexane and clean gasoline blend component.
Description
Technical field
The present invention relates to a kind of methods for producing n-hexane and clean gasoline blend component, and in particular to a kind of using hydrogenation
The method of the high additional n-hexane of rectification process manufacture and clean gasoline blend component.
Background technology
Benzene,toluene,xylene is industrially commonly called as triphen, as industrial chemicals or solvent, is widely used in dye industry, agriculture
The industries such as industry generation, fragrance manufacture, pharmacy.It is mainly produced at present using catalytic reforming technology, still, since technology limits
System, the yield of the aromatic hydrocarbons especially benzene of catalytic reforming unit is relatively low, also has substantial portion of by-product, that is, Aromatic raffinate, accounts for
The 30~40% of reformed oil.Aromatic raffinate (boiling range≤90 DEG C) is based on the saturated hydrocarbons of C6~C8, n-hexane content 20
~30%, total isomery hydrocarbon content 65~75%, containing a small amount of alkene, arene content is low, and sulphur, nitrogen and beavy metal impurity content are extremely low.
Reformed arene is raffinated oil mainly for the production of all kinds of good solvent naphthas and the hexane of high added value oil at present；Due to aromatic hydrocarbons raffinate
Oily octane number (RON) only has 60~70, limited as gasoline blend component addition, and as solvent naphtha use added value compared with
It is low.
The content of the invention
There is provided it is an object of the invention to overcome in place of the shortcomings of the prior art a kind of Joint Production n-hexane and
The method of clean gasoline blend component.
To achieve the above object, the technical solution taken of the present invention is：A kind of Joint Production n-hexane and clean gasoline tune
With the method for component, comprise the following steps：
(1), Aromatics Extractive Project by-product is added in fiber-film contact, desulfurization process；
(2), the product after desulfurization process is carried out dehydrating；
(3), the product after dehydration is subjected to hydrotreating；
(4), the product after hydrotreating is subjected to rectifying separation, obtains the n-hexane and clean gasoline blend component.
Aromatics Extractive Project by-product of the present invention refers in petroleum refining process, the reformation rich in aromatic hydrocarbons C6~C8 components
Generation oil distillate obtained after Aromatics Extractive Project, main component are the saturated hydrocarbons of C6~C8 and a small amount of alkene and virtue
Hydrocarbon.
The present invention be using Aromatics Extractive Project by-product as raw material, due to containing a small amount of sulphur in raw material, sulfur content for 50~
100PPM, the sulfolane (extraction solvent) mainly carried secretly in aromatics extraction process, using sulfolane it is miscible with water the characteristics of, adopt
Washed with softened water by fiber-film contact and remove sulfolane, then remove moisture, then by hydrogenation reaction remove alkene and
Aromatic hydrocarbons, reaction product obtain n-hexane and clean gasoline blend component after rectifying separates, and the content of the n-hexane of acquisition >=
70%.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, step
Suddenly after (3) and before step (4), also comprising step (3a)：Material cools down through hydrogenated processing into heat exchanger afterwards, then passes through
The product after hydrotreating is obtained after gas-liquid separator.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, step
Suddenly in (1), the oil-water ratio of desulfurization process is 10 in the fiber-film contact:2~4.
If oil-water ratio is excessive, power cost is higher, if oil-water ratio is too small, desulfurization effect is poor.It is repeatedly anti-through inventor
Retrial, which is tested, to draw, during using above-mentioned oil-water ratio, can ensure desulfuration efficiency while desulfurization effect is ensured.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, step
Suddenly in (1), the operation temperature in the fiber-film contact is 35~45 DEG C, 0.1~0.25MPa of operating pressure, the fiber
The pressure drop of membrane contactor is 0.06~0.08MPa.
In product after the desulfurization obtained under the operating conditions described above, sulfur content is less than 0.5PPM.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, step
Suddenly in (2), the device that the dehydration uses is molecular sieve water separation tower.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, institute
State moisture≤50PPM of the product after dehydration.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, step
Suddenly in (3), device that the hydrotreating uses for two series connection hydrogenation reactor：Hydrogenation reactor I and hydrogenation reactor
II。
The hydrogenation reactor I is for removing alkene；The hydrogenation reactor II is for removing aromatic hydrocarbons.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, institute
The reaction pressure of hydrogenation reactor I is stated as 1.80~2.20MPa, reaction temperature is 155~165 DEG C, and air speed is 2~4h-1, hydrogen
Volume ratio with the product after dehydration is：Hydrogen：Product=500~800 after dehydration:1.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, institute
The reaction pressure of hydrogenation reactor II is stated as 1.80~2.00MPa, reaction temperature is 150~165 DEG C, and air speed is 2~3h-1, hydrogen
The volume ratio of product after gas and dehydration is：Hydrogen：Product=300~500 after dehydration:1.
In the present invention, the volume ratio of the product after hydrogen and dehydration is known as hydrogen-oil ratio.Hydrogen-oil ratio is crossed conference and is enabled
Consumption increase, device operating cost are excessively high；Hydrogen-oil ratio is too small so that hydrogenation reaction is incomplete, influences product quality.
The hydrotreating of the present invention carries out hydrotreating, hydrogenation efficiency under these conditions using two-part hydrotreating
Height, for the product bromine index after hydrotreating no more than 5mgBr/100g, benzene content is less than 50PPM.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, step
Suddenly in (4), the rectifying separates the rectifying column that the device used is connected for two：First rectifying column and Second distillation column；It is described
The operating condition of first rectifying column is：Feeding temperature is 35~45 DEG C, and tower top temperature is 62~66 DEG C, and column bottom temperature is 75~82
DEG C, overhead reflux temperature is 30~40 DEG C, and overhead reflux ratio is 60~80, and the operation absolute pressure of tower is 0.10~0.12MPa；
The operating condition of Second distillation column is：Feeding temperature is 70~80 DEG C, and tower top temperature is 60~63 DEG C, and column bottom temperature is 79~85
DEG C, overhead reflux temperature is 30~40 DEG C, and overhead reflux ratio is 50~70, and the operation absolute pressure of tower is 0.10~0.12MPa.
As Joint Production n-hexane of the present invention and the preferred embodiment of the method for clean gasoline blend component, institute
It is 28 to state the ratio between Gao Jing of first rectifying column:1, the ratio between Gao Jing of Second distillation column are 30:1 first rectifying column and the second essence
The tower internals for evaporating tower is arranged in pairs or groups using the silk screen and ripple packing of structured filling material layer, and silk screen and the ripple of the structured filling material layer are filled out
The weight ratio of material is：The silk screen of structured filling material layer：Ripple packing=1.5:1.
Since reformed arene octane number (RON) of raffinating oil is relatively low, only 60~70, contain in reformed arene raffinate oil ingredient
20~30% n-hexane, the octane number (RON) of n-hexane only have 25, can be carried using the silk screen and ripple packing of structured filling material layer
High separating efficiency, extracts the relatively low component (n-hexane) of octane number from raw material to greatest extent, and the isoparaffin for improving product contains
Amount, correspondingly improves its octane number.
The advantageous effect of method of the present invention is：The present invention provides a kind of Joint Production n-hexanes and cleaning vapour
The method of oily blend component, this method is be combined with each other using different technical process, and the n-hexane of consecutive production high-quality
And good gasoline blend component, compared with the treatment process of traditional Aromatic raffinate, obtained added value of product higher；Just
Hexane content is more than 70%, boiling range narrow range (66~70 DEG C)；Gasoline blend component octane number (RON) is more than 86, benzene content
Less than 50PPM, sulfur content is not more than 0.5PPM, and bromine index is not more than 5mgBr/100g.Joint Production n-hexane of the present invention
Aromatics Extractive Project by-product is farthest rationally make use of with the method for clean gasoline blend component, is avoided in conventional production practices
The solvent oil processing relatively low as added value of product after middle acquisition hexane-fraction, can obtain low-sulfur, higher octane number
Blend component can be alleviated now to the demand pressure of clean gasoline, be a kind of high value added utilization Aromatics Extractive Project by-product to make
The new process of standby n-hexane and clean gasoline blend component.
Specific embodiment
Embodiment 1
A kind of embodiment of the method for Joint Production n-hexane and clean gasoline blend component of the present invention, the present embodiment
The method of the Joint Production n-hexane and clean gasoline blend component comprises the following steps：
(1), Aromatics Extractive Project by-product is added in fiber-film contact, the ring carried by washing removing Aromatic raffinate
Fourth sulfone, operating condition are that oil-water ratio is 10:4, operation temperature is 40 DEG C, operating pressure 0.25MPa, fiber-film contact pressure drop
For 0.06MPa；
(2), the product after desulfurization process is carried out dehydrating in through molecular sieve water separation tower；
(3), the product after dehydration is sequentially entered into hydrogenation reactor I and hydrogenation reactor II and carries out hydrotreating,
Hydrogenation reactor I carries out deolefination processing, and deolefination reactor reaction pressure is 1.80MPa, and reaction temperature is 155 DEG C, air speed
For 2h-1, hydrogen-oil ratio 500:1；Hydrogenation reactor II carries out Porous deproteinized bone processing, and Porous deproteinized bone reactor reaction pressure is 1.80MPa,
Reaction temperature is 160 DEG C, air speed 2h-1, hydrogen-oil ratio 300:1；It cools down through heat exchanger, then is added through gas-liquid separator separates
Hydrogen treated product, hydrogen send to hydrogenation reactor and recycle；
(4), the product after hydrotreating enters the rectifying column of two series connection：First rectifying column and Second distillation column；It is described
The ratio between Gao Jing of first rectifying column is 28:1, the ratio between Gao Jing of the Second distillation column is 30:1, the first rectifying column and
The tower internals of two rectifying columns is arranged in pairs or groups using the silk screen of structured filling material layer with ripple packing, the silk screen and ripple of the structured filling material layer
The weight ratio of filler is：The silk screen of structured filling material layer：Ripple packing=1.5:1；The operating condition of first rectifying column is：Charging
Temperature is 36 DEG C, and tower top temperature is 62 DEG C, and column bottom temperature is 78 DEG C, and overhead reflux temperature is 35 DEG C, and overhead reflux ratio is 60, tower
Operation absolute pressure be 0.10MPa；The operating condition of Second distillation column is：Feeding temperature is 70 DEG C, and tower top temperature is 60 DEG C,
Column bottom temperature is 82 DEG C, and overhead reflux temperature is 30 DEG C, and overhead reflux ratio is 50, and the operation absolute pressure of tower is 0.11MPa.,
The tower top of Second distillation column tower top isolates n-hexane, and remaining ingredient is good gasoline blend component, obtain the n-hexane and
Clean gasoline blend component.
Embodiment 2
A kind of embodiment of the method for Joint Production n-hexane and clean gasoline blend component of the present invention, the present embodiment
The method of the Joint Production n-hexane and clean gasoline blend component comprises the following steps：
(1), Aromatics Extractive Project by-product is added in fiber-film contact, the ring carried by washing removing Aromatic raffinate
Fourth sulfone, operating condition are that oil-water ratio is 10:2, operation temperature is 35 DEG C, operating pressure 0.20MPa, fiber-film contact pressure drop
For 0.08MPa；
(2), the product after desulfurization process is carried out dehydrating in through molecular sieve water separation tower；
(3), the product after dehydration is sequentially entered into hydrogenation reactor I and hydrogenation reactor II and carries out hydrotreating,
Hydrogenation reactor I carries out deolefination processing, and deolefination reactor reaction pressure is 1.90MPa, and reaction temperature is 160 DEG C, air speed
For 3h-1, hydrogen-oil ratio 600:1；Hydrogenation reactor II carries out Porous deproteinized bone processing, and Porous deproteinized bone reactor reaction pressure is 1.90MPa,
Reaction temperature is 155 DEG C, air speed 2.5h-1, hydrogen-oil ratio 400:1；It cools down through heat exchanger, then is obtained through gas-liquid separator separates
Product after hydrotreating, hydrogen send to hydrogenation reactor and recycle；
(4), the product after hydrotreating enters the rectifying column of two series connection：First rectifying column and Second distillation column；It is described
The ratio between Gao Jing of first rectifying column is 28:1, the ratio between Gao Jing of the Second distillation column is 30:1, the first rectifying column and
The tower internals of two rectifying columns is arranged in pairs or groups using the silk screen of structured filling material layer with ripple packing, the silk screen and ripple of the structured filling material layer
The weight ratio of filler is：The silk screen of structured filling material layer：Ripple packing=1.5:1；First rectifying column operating condition is：Into material temperature
It spends for 38 DEG C, tower top temperature is 63 DEG C, and column bottom temperature is 80 DEG C, and overhead reflux temperature is 40 DEG C, and overhead reflux ratio is 70, tower
Operation absolute pressure is 0.11MPa；Second distillation column operating condition is：Feeding temperature is 72 DEG C, and tower top temperature is 61 DEG C, bottom of towe
Temperature is 83 DEG C, and overhead reflux temperature is 35 DEG C, and overhead reflux ratio is 60, and the operation absolute pressure of tower is 0.11MPa., second
The tower top of rectifying column tower top isolates n-hexane, and remaining ingredient is good gasoline blend component, obtains the n-hexane and cleaning
Gasoline blend component.
Embodiment 3
A kind of embodiment of the method for Joint Production n-hexane and clean gasoline blend component of the present invention, the present embodiment
The method of the Joint Production n-hexane and clean gasoline blend component comprises the following steps：
(1), Aromatics Extractive Project by-product is added in fiber-film contact, the ring carried by washing removing Aromatic raffinate
Fourth sulfone, operating condition are that oil-water ratio is 10:3, operation temperature is 40 DEG C, operating pressure 0.22MPa, fiber-film contact pressure drop
For 0.07MPa；
(2), the product after desulfurization process is carried out dehydrating in through molecular sieve water separation tower；
(3), the product after dehydration is sequentially entered into hydrogenation reactor I and hydrogenation reactor II and carries out hydrotreating,
Hydrogenation reactor I carries out deolefination processing, and deolefination reactor reaction pressure is 2.10MPa, and reaction temperature is 160 DEG C, air speed
For 4h-1, hydrogen-oil ratio 700:1；Hydrogenation reactor II carries out Porous deproteinized bone processing, and Porous deproteinized bone reactor reaction pressure is 2.00MPa,
Reaction temperature is 160 DEG C, air speed 3h-1, hydrogen-oil ratio 400:1；It cools down through heat exchanger, then is added through gas-liquid separator separates
Hydrogen treated product, hydrogen send to hydrogenation reactor and recycle；
(4), the product after hydrotreating enters the rectifying column of two series connection：First rectifying column and Second distillation column；It is described
The ratio between Gao Jing of first rectifying column is 28:1, the ratio between Gao Jing of the Second distillation column is 30:1, the first rectifying column and
The tower internals of two rectifying columns is arranged in pairs or groups using the silk screen of structured filling material layer with ripple packing, the silk screen and ripple of the structured filling material layer
The weight ratio of filler is：The silk screen of structured filling material layer：Ripple packing=1.5:1；The operating condition of first rectifying column is：Charging
Temperature is 40 DEG C, and tower top temperature is 64 DEG C, and column bottom temperature is 81 DEG C, and overhead reflux temperature is 40 DEG C, and overhead reflux ratio is 70, tower
Operation absolute pressure be 0.11MPa；The operating condition of Second distillation column is：Feeding temperature is 72 DEG C, and tower top temperature is 62 DEG C,
Column bottom temperature is 83 DEG C, and overhead reflux temperature is 40 DEG C, and overhead reflux ratio is 70, and the operation absolute pressure of tower is 0.11MPa.,
The tower top of Second distillation column tower top isolates n-hexane, and remaining ingredient is good gasoline blend component, obtain the n-hexane and
Clean gasoline blend component.
Embodiment 4
A kind of embodiment of the method for Joint Production n-hexane and clean gasoline blend component of the present invention, the present embodiment
The method of the Joint Production n-hexane and clean gasoline blend component comprises the following steps：
(1), Aromatics Extractive Project by-product is added in fiber-film contact, the ring carried by washing removing Aromatic raffinate
Fourth sulfone, operating condition are that oil-water ratio is 10:3, operation temperature is 45 DEG C, operating pressure 0.1MPa, fiber-film contact pressure drop
For 0.07MPa；
(2), the product after desulfurization process is carried out dehydrating in through molecular sieve water separation tower；
(3), the product after dehydration is sequentially entered into hydrogenation reactor I and hydrogenation reactor II and carries out hydrotreating,
Hydrogenation reactor I carries out deolefination processing, and deolefination reactor reaction pressure is 2.20MPa, and reaction temperature is 160 DEG C, air speed
For 4h-1, hydrogen-oil ratio 800:1；Hydrogenation reactor II carries out Porous deproteinized bone processing, and Porous deproteinized bone reactor reaction pressure is 2.00MPa,
Reaction temperature is 160 DEG C, air speed 3h-1, hydrogen-oil ratio 500:1；It cools down through heat exchanger, then is added through gas-liquid separator separates
Hydrogen treated product, hydrogen send to hydrogenation reactor and recycle；
(4), the product after hydrotreating enters the rectifying column of two series connection：First rectifying column and Second distillation column；It is described
The ratio between Gao Jing of first rectifying column is 28:1, the ratio between Gao Jing of the Second distillation column is 30:1, the first rectifying column and
The tower internals of two rectifying columns is arranged in pairs or groups using the silk screen of structured filling material layer with ripple packing, the silk screen and ripple of the structured filling material layer
The weight ratio of filler is：The silk screen of structured filling material layer：Ripple packing=1.5:1；The operating condition of first rectifying column is：Charging
Temperature is 45 DEG C, and tower top temperature is 65 DEG C, and column bottom temperature is 82 DEG C, and overhead reflux temperature is 40 DEG C, and overhead reflux ratio is 80, tower
Operation absolute pressure be 0.12MPa；The operating condition of Second distillation column is：Feeding temperature is 75 DEG C, and tower top temperature is 63 DEG C,
Column bottom temperature is 84 DEG C, and overhead reflux temperature is 35 DEG C, and overhead reflux ratio is 70, and the operation absolute pressure of tower is 0.12MPa.,
The tower top of Second distillation column tower top isolates n-hexane, and remaining ingredient is good gasoline blend component, obtain the n-hexane and
Clean gasoline blend component.
Embodiment 5
N-hexane obtained by Examples 1 to 4 and clean gasoline blend component are subjected to dependence test analysis, test result
See Tables 1 and 2.
1 n-hexane interpretation of result of table
2 clean gasoline blend component interpretation of result of table
As can be seen from Table 1 and Table 2, the method for Joint Production n-hexane and clean gasoline blend component of the present invention can
To maximize rationally using Aromatic raffinate, the n-hexane of high added value and good clean gasoline blend component are produced.
Finally, it should be noted that the above embodiments are merely illustrative of the technical solutions of the present invention rather than the present invention is protected
The limitation of scope is protected, although being explained in detail with reference to preferred embodiment to the present invention, those of ordinary skill in the art should
Understand, technical scheme can be modified or replaced equivalently, without departing from the essence of technical solution of the present invention
And scope.
Claims (10)
1. a kind of method of Joint Production n-hexane and clean gasoline blend component, which is characterized in that comprise the following steps：
(1), Aromatics Extractive Project by-product is added in fiber-film contact, desulfurization process；
(2), the product after desulfurization process is carried out dehydrating；
(3), the product after dehydration is subjected to hydrotreating；
(4), the product after hydrotreating is subjected to rectifying separation, obtains the n-hexane and clean gasoline blend component.
2. the method for Joint Production n-hexane as described in claim 1 and clean gasoline blend component, which is characterized in that step
(1) in, the oil-water ratio of desulfurization process is 10 in the fiber-film contact:2~4.
3. the method for Joint Production n-hexane as described in claim 1 and clean gasoline blend component, which is characterized in that step
(1) in, the operation temperature in the fiber-film contact is 35~45 DEG C, 0.1~0.25MPa of operating pressure, the tunica fibrosa
The pressure drop of contactor is 0.06~0.08MPa.
4. the method for Joint Production n-hexane as described in claim 1 and clean gasoline blend component, which is characterized in that step
(2) in, the device that the dehydration uses is molecular sieve water separation tower.
5. the method for Joint Production n-hexane as described in claim 1 and clean gasoline blend component, which is characterized in that described de-
Moisture≤50PPM of product after water process.
6. the method for Joint Production n-hexane as described in claim 1 and clean gasoline blend component, which is characterized in that step
(3) in, device that the hydrotreating uses for two series connection hydrogenation reactor：Hydrogenation reactor I and hydrogenation reactor II.
7. the method for Joint Production n-hexane as claimed in claim 6 and clean gasoline blend component, which is characterized in that described to add
The reaction pressure of hydrogen reactor I is 1.80~2.20MPa, and reaction temperature is 155~165 DEG C, and air speed is 2~4h-1, hydrogen and de-
The volume ratio of product after water process is：Hydrogen：Product=500~800 after dehydration:1.
8. the method for Joint Production n-hexane as claimed in claim 6 and clean gasoline blend component, which is characterized in that described to add
The reaction pressure of hydrogen reactor II is 1.80~2.00MPa, and reaction temperature is 150~165 DEG C, and air speed is 2~3h-1, hydrogen and
The volume ratio of product after dehydration is：Hydrogen：Product=300~500 after dehydration:1.
9. the method for Joint Production n-hexane as described in claim 1 and clean gasoline blend component, which is characterized in that step
(4) in, the rectifying separates the rectifying column that the device used is connected for two：First rectifying column and Second distillation column；Described
The operating condition of one rectifying column is：Feeding temperature is 35~45 DEG C, and tower top temperature is 62~66 DEG C, and column bottom temperature is 75~82
DEG C, overhead reflux temperature is 30~40 DEG C, and overhead reflux ratio is 60~80, and the operation absolute pressure of tower is 0.10~0.12MPa；
The operating condition of Second distillation column is：Feeding temperature is 70~80 DEG C, and tower top temperature is 60~63 DEG C, and column bottom temperature is 79~85
DEG C, overhead reflux temperature is 30~40 DEG C, and overhead reflux ratio is 50~70, and the operation absolute pressure of tower is 0.10~0.12MPa.
10. the method for Joint Production n-hexane as claimed in claim 9 and clean gasoline blend component, which is characterized in that described
The ratio between Gao Jing of first rectifying column is 28:1, the ratio between Gao Jing of Second distillation column are 30:1；The first rectifying column and the second essence
The tower internals for evaporating tower is arranged in pairs or groups using the silk screen and ripple packing of structured filling material layer, and silk screen and the ripple of the structured filling material layer are filled out
The weight ratio of material is：The silk screen of structured filling material layer：Ripple packing=1.5:1.
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| CN1569782A (en) * | 2004-04-27 | 2005-01-26 | 广州赫尔普化工有限公司 | Method for preparing isohexane solvent |
| CN101148390A (en) * | 2007-10-12 | 2008-03-26 | 中国石化扬子石油化工有限公司 | Technique for extracting high-pure normal hexane product by pressure swing adsorption |
| CN101608133A (en) * | 2009-06-18 | 2009-12-23 | 广州中元石油化工工程有限公司 | The manufacture method of one vegetable oil extraction solvent |
| CN102212392A (en) * | 2011-05-10 | 2011-10-12 | 广州赫尔普化工有限公司 | Preparation method of edible oil leaching agent |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1569782A (en) * | 2004-04-27 | 2005-01-26 | 广州赫尔普化工有限公司 | Method for preparing isohexane solvent |
| CN101148390A (en) * | 2007-10-12 | 2008-03-26 | 中国石化扬子石油化工有限公司 | Technique for extracting high-pure normal hexane product by pressure swing adsorption |
| CN101608133A (en) * | 2009-06-18 | 2009-12-23 | 广州中元石油化工工程有限公司 | The manufacture method of one vegetable oil extraction solvent |
| CN102212392A (en) * | 2011-05-10 | 2011-10-12 | 广州赫尔普化工有限公司 | Preparation method of edible oil leaching agent |
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