CN105112098B - A kind of hydrofinishing process of solvent naphtha - Google Patents
A kind of hydrofinishing process of solvent naphtha Download PDFInfo
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- CN105112098B CN105112098B CN201510506133.0A CN201510506133A CN105112098B CN 105112098 B CN105112098 B CN 105112098B CN 201510506133 A CN201510506133 A CN 201510506133A CN 105112098 B CN105112098 B CN 105112098B
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Abstract
The present invention relates to a kind of hydrofinishing process of solvent naphtha, more particularly to a kind of hydrofinishing process of printing oil solvent.The hydrofinishing process of this solvent naphtha comprises the following steps：Raw material pre-treatment, a hydrofinishing, secondary hydrofinishing, the cutting of accurate cut.It is raw material that the present invention, which chooses shale oil and the mixture of coal tar, utilize two step progressive crackings, the double reaction bed hydrogenation techniques of suspension bed slurry bed system, now the heavy oil composition in mixing oil product fully thoroughly crack and be converted into light-end products, make the oxygen in mixing oil product simultaneously, sulphur, nitrogen and metal impurities are able to partial removal alkene and aromatic compound and saturation, improve the quality of intermediate, and improve the heat of final product, light stability, it is poor to overcome aliphatic ink solvent power, the defects of aromatic hydrocarbon ink solvent toxicity is big, and reduce harm of the ink in use to environment and human body, it is widely used in offset printing and letterpress printing ink.
Description
Technical field
The present invention relates to a kind of hydrofinishing process of solvent naphtha, more particularly to a kind of hydrofinishing side of printing oil solvent
Method.
Background technology
Printing oil solvent is the primary raw material for producing ink, accounts for the 60% of ink total raw material.Offset printing ink solvent oil is glue
The important component of stamp-pad ink ink connecting material.It is neither the true solvent of offset plate ink resin, nor its cosolvent, but
Play diluent, binder is diluted by means of printing oil solvent so that manufactured ink viscosity declines, in ink
Charge is 30% or so.In printing process, after the printing oil solvent in ink is penetrated into paper, ink is enabled to
It is rapid to dry, the set speed of ink is improved, adapts to the needs of high speed printing.Existing printing oil solvent, belongs to petroleum more
Product, mainly obtain appropriate fractions, then the production obtained through different processing technologys through distillation by paraffinic base and the crude oil of cycloalkyl
Product, its processing method are summarised as four kinds:The first processing method is that the direct steaming gasoline obtained with paraffinic base crude oil air-distillation evaporates
It is divided into raw material, the product obtained after refined and rectifying.Second of processing method is obtained with paraffinic base crude oil air-distillation
Straight-run is raw material, the product obtained after cold press dewaxing, hydrofinishing.The third production method is with naphthene base crude
Appropriate fractions are the product that raw material obtains after distilling, reconciling.4th kind of production method is taken out with the lubricating oil of naphthene base crude
The fuel-displaced product obtained for raw material after distilling, reconciling.The product aniline point that first three methods obtain is high, molten with ink resin
Solution property is poor, and so as to must more use expensive true solvent, dry vegetable oil strengthens dicyandiamide solution to the molten of resin
Solution ability, it certainly will so increase the cost of ink.The product that 4th kind of method obtains, pour point high and low temperature poor fluidity, is applied to
Its fast solvent release performance is undesirable in offset printing colored ink.
The content of the invention
The technical problem to be solved in the present invention is how to overcome the drawbacks described above of prior art, there is provided a kind of solvent naphtha adds
Hydrogen process for purification.
In order to solve the above technical problems, the hydrofinishing process of this solvent naphtha comprises the following steps：
Step (1) --- raw material pre-treatment：The raw material is the mixture of shale oil and coal tar, parts by weights ratio
Count, the weight ratio of shale oil and coal tar is 5~10 in the mixture of the shale oil and coal tar：1, by shale oil and
The mixture of coal tar carries out high-temperature low-pressure distillation, quick separating under 300~400 DEG C of temperature, 0.05~0.08MPa of pressure
Obtain light oil and mink cell focus；
Step (2) a --- hydrofinishing：The isolated mink cell focus of step (1) is carried out in bubbling bed reactor
Hydrofining reaction, the addition of Hydrobon catalyst is to control the total metal content of active component and enter suspended-bed reactor
Mink cell focus weight ratio be 1.0~1.5：100, produce a hydrofined oil；
Step (3) --- secondary hydrofinishing：The isolated light oil of step (1) and step (2) are obtained once
Hydrofined oil is well mixed, and carries out secondary hydrofinishing in paste state bed reactor, the addition of Hydrobon catalyst with
The weight ratio for controlling mink cell focus of the total metal content of active component with entering bubbling bed reactor is 3~8：100, produce two
Secondary hydrofined oil；
Step (4) --- accurate cut cutting：Secondary hydrofined oil precision fractionation made from step (3) is cut out
250~350 DEG C of cuts, produce this solvent naphtha.
As prioritization scheme：Step (2) hydrofining reaction condition is --- temperature is 200~300 DEG C, pressure
Power is 10.0~15.0MPa, volume space velocity is 0.2~0.5h-1, hydrogen to oil volume ratio 1000~1500：1.
As prioritization scheme：Step (2) the secondary hydrofining reaction condition is --- temperature is 300~400 DEG C, pressure
Power is 15.0~25.0MPa, volume space velocity is 0.5~1.0h-1, hydrogen to oil volume ratio 1500~2000：1.
As prioritization scheme：Step (4) process conditions by secondary hydrofined oil precision fractionation are --- tower top
180~200 DEG C of temperature, tower top pressure -0.05~-0.10MPa, 200~225 DEG C of column bottom temperature.
As prioritization scheme：The preparation method of Hydrobon catalyst described in step (2) and step (3) is first will
Nickelous carbonate is made by sol-gal process, then in 500~650 DEG C of 3~5h of roasting of temperature, obtains nickel oxide, the oxygen that will be obtained
Change nickel with aluminum oxide with 0.5~1：1 ratio extruding is integrated, in 150~200 DEG C of dry 5~8h of temperature, then at temperature 600
5~8h is calcined at~750 DEG C, obtains carrier, the metal that the carrier is soaked in the nickel that oxidation nickel concentration is 0.5~1.5g/L is molten
24h in liquid, after taking-up, 3~5h, the dry 5~8h of 150~200 DEG C of temperature are calcined at 500~650 DEG C of temperature.
A kind of hydrofinishing process of solvent naphtha of the present invention, the mixture for choosing shale oil and coal tar is raw material, is utilized
The double reaction bed hydrogenation techniques of two step progressive crackings, suspension bed slurry bed system, now the heavy oil composition in mixing oil product is carried out abundant
Thoroughly cracking is converted into light-end products, while enables oxygen, sulphur, nitrogen and the metal impurities partial removal alkene in mixing oil product
And aromatic compound and saturation, the quality of intermediate is improved, and improve the heat of final product, light stability, overcome fat
The defects of race's printing ink solvent dissolving power is poor, aromatic hydrocarbon ink solvent toxicity is big, and ink is reduced in use to ring
Border and the harm of human body, are widely used in offset printing and letterpress printing ink.
Embodiment
Embodiment：The hydrofinishing process of this solvent naphtha comprises the following steps,
Step (1) --- raw material pre-treatment：The raw material is the mixture of shale oil and coal tar, parts by weights ratio
Count, the weight ratio of shale oil and coal tar is 5~10 in the mixture of the shale oil and coal tar：1, by shale oil and
The mixture of coal tar carries out high-temperature low-pressure distillation, quick separating under 300~400 DEG C of temperature, 0.05~0.08MPa of pressure
Obtain light oil and mink cell focus；
Step (2) a --- hydrofinishing：The isolated mink cell focus of step (1) is carried out in bubbling bed reactor
Hydrofining reaction, the addition of Hydrobon catalyst is to control the total metal content of active component and enter suspended-bed reactor
Mink cell focus weight ratio be 1.0~1.5：100, produce a hydrofined oil；
Step (3) --- secondary hydrofinishing：The isolated light oil of step (1) and step (2) are obtained once
Hydrofined oil is well mixed, and carries out secondary hydrofinishing in paste state bed reactor, the addition of Hydrobon catalyst with
The weight ratio for controlling mink cell focus of the total metal content of active component with entering bubbling bed reactor is 3~8：100, produce two
Secondary hydrofined oil；
Step (4) --- accurate cut cutting：Secondary hydrofined oil precision fractionation made from step (3) is cut out
250~350 DEG C of cuts, produce this solvent naphtha.
Above-mentioned steps (2) hydrofining reaction condition is --- temperature is 200~300 DEG C, pressure 10.0
~15.0MPa, volume space velocity are 0.2~0.5h-1, hydrogen to oil volume ratio 1000~1500：1.
Above-mentioned steps (2) the secondary hydrofining reaction condition is --- temperature is 300~400 DEG C, pressure 15.0
~25.0MPa, volume space velocity are 0.5~1.0h-1, hydrogen to oil volume ratio 1500~2000：1.
Above-mentioned steps (4) process conditions by secondary hydrofined oil precision fractionation are --- tower top temperature 180~
200 DEG C, tower top pressure -0.05~-0.10MPa, 200~225 DEG C of column bottom temperature.
The preparation method of Hydrobon catalyst described in above-mentioned steps (2) and step (3) is that will be coagulated first by colloidal sol
Glue legal system obtains nickelous carbonate, then in 500~650 DEG C of 3~5h of roasting of temperature, nickel oxide is obtained, by obtained nickel oxide and oxidation
Aluminium is with 0.5~1：1 ratio extruding is integrated, and in 150~200 DEG C of dry 5~8h of temperature, is roasted at 600~750 DEG C of temperature
5~8h is burnt, obtains carrier, the carrier is soaked in 24h in the metallic solution for the nickel that oxidation nickel concentration is 0.5~1.5g/L, taken
After going out, 3~5h, the dry 5~8h of 150~200 DEG C of temperature are calcined at 500~650 DEG C of temperature.
It can be that professional and technical personnel in the field realize or used that above-mentioned embodiment, which is intended to illustrate the present invention, to above-mentioned
Embodiment is modified and will be apparent for those skilled in the art, therefore the present invention includes but is not limited to
Above-mentioned embodiment, it is any to meet the claims or specification description, meet with principles disclosed herein and novelty,
The method of inventive features, technique, product, each fall within protection scope of the present invention.
Claims (1)
1. a kind of hydrofinishing process of solvent naphtha, it is characterized in that：The hydrofinishing process of the solvent naphtha comprises the following steps：
Step (1) --- raw material pre-treatment：The raw material is the mixture of shale oil and coal tar, parts by weights ratio meter, institute
It is 5~10 to state the weight ratio of shale oil and coal tar in the mixture of shale oil and coal tar：1, by shale oil and coal tar
The mixture of oil carries out high-temperature low-pressure distillation under 300~400 DEG C of temperature, 0.05~0.08MPa of pressure, and quick separating obtains gently
Matter oil and mink cell focus；
Step (2) a --- hydrofinishing：The isolated mink cell focus of step (1) is hydrogenated with suspended-bed reactor
Refining reaction, the weight of the addition of Hydrobon catalyst to control the total metal content of active component with enter suspended-bed reactor
The weight ratio of matter oil is 1.0~1.5：100, produce a hydrofined oil；Hydrofining reaction condition
For --- temperature is 200~300 DEG C, pressure is 10.0~15.0MPa, volume space velocity is 0.2~0.5h-1, hydrogen to oil volume ratio
1000~1500：1；The preparation method of described Hydrobon catalyst is that nickelous carbonate will be made by sol-gal process first,
Then in 500~650 DEG C of 3~5h of roasting of temperature, nickel oxide is obtained, by obtained nickel oxide and aluminum oxide with 0.5~1：1 ratio
Example extruding is integrated, and in 150~200 DEG C of drys 5~8h of temperature, then at 5~8h of roasting at 600~750 DEG C of temperature, is carried
Body, the carrier is soaked in 24h in the metallic solution for the nickel that oxidation nickel concentration is 0.5~1.5g/L, after taking-up, in temperature 500
3~5h, the dry 5~8h of 150~200 DEG C of temperature are calcined at~650 DEG C；
Step (3) --- secondary hydrofinishing：The once hydrogenation that the isolated light oil of step (1) and step (2) are obtained
Refined oil is well mixed, and carries out secondary hydrofinishing in paste state bed reactor, and the addition of Hydrobon catalyst is to control
The weight ratio of mink cell focus of the total metal content of active component with entering paste state bed reactor is 3~8：100, produce secondary add
Hydrogen refined oil；The preparation method of described Hydrobon catalyst is that nickelous carbonate will be made by sol-gal process first, then
In 500~650 DEG C of 3~5h of roasting of temperature, nickel oxide is obtained, by obtained nickel oxide and aluminum oxide with 0.5~1：1 ratio is squeezed
Consolidation, in 150~200 DEG C of dry 5~8h of temperature, 5~8h is calcined at 600~750 DEG C of temperature, obtains carrier, will
The carrier is soaked in 24h in the metallic solution for the nickel that oxidation nickel concentration is 0.5~1.5g/L, after taking-up, in temperature 500~650
3~5h, the dry 5~8h of 150~200 DEG C of temperature are calcined at DEG C；The secondary hydrofining reaction condition is --- temperature 300
~400 DEG C, pressure be 15.0~25.0MPa, volume space velocity be 0.5~1.0h-1, hydrogen to oil volume ratio 1500~2000：1；
Step (4) --- accurate cut cutting：Secondary hydrofined oil precision fractionation made from step (3) is cut out 250~
350 DEG C of cuts, produce this solvent naphtha；The process conditions by secondary hydrofined oil precision fractionation are --- tower top temperature
180~200 DEG C, tower top pressure -0.05~-0.10MPa, 200~225 DEG C of column bottom temperature.
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| CN201510506133.0A CN105112098B (en) | 2015-08-17 | 2015-08-17 | A kind of hydrofinishing process of solvent naphtha |
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| CN201510506133.0A CN105112098B (en) | 2015-08-17 | 2015-08-17 | A kind of hydrofinishing process of solvent naphtha |
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| CN105112098B true CN105112098B (en) | 2018-01-26 |
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| CN102703116B (en) * | 2012-05-29 | 2014-06-18 | 煤炭科学研究总院 | Ink solvent oil and preparation method thereof |
| CN102807899B (en) * | 2012-07-26 | 2015-03-25 | 煤炭科学研究总院 | Coal-based environment-friendly solvent oil and preparation method thereof |
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Effective date of registration: 20190306 Address after: 261300 Chengtai Road, Binhai (Xiaying) Economic Development Zone, Changyi City, Weifang City, Shandong Province Patentee after: Shandong Chengtai New Materials Co., Ltd. Address before: 261313 Binhai (Xiaying) Economic Development Zone, Weifang City, Shandong Province Patentee before: Shandong Cheng Tai Chemical Co., Ltd. |