CN109722304A - A kind of production method of hydraulic oil - Google Patents
A kind of production method of hydraulic oil Download PDFInfo
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- CN109722304A CN109722304A CN201910083029.3A CN201910083029A CN109722304A CN 109722304 A CN109722304 A CN 109722304A CN 201910083029 A CN201910083029 A CN 201910083029A CN 109722304 A CN109722304 A CN 109722304A
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Abstract
The invention discloses a kind of production method of hydraulic oil, carry out being heated to the first preset temperature after feedstock oil is mixed with hydrogen；It is then introduced into the isomerizing reactor equipped with shape-selective heterogeneous catalyst to be reacted to obtain primary first-order equation effluent, and shape-selective heterogeneous catalyst is the mixture of molecular sieve and the shape-selective heterogeneous catalyst of platinum palladium noble metal；Primary first-order equation effluent progress temperature is adjusted to import in the post-refining reactor containing refining reaction catalyst after the second preset temperature and is reacted to obtain secondary response effluent, and refining reaction catalyst is the mixture of molecular sieve and platinum palladium noble metal post-refining catalyst；Gas liquid separation is carried out to secondary response effluent, to obtain recycling hydrogen and liquid product；Fractionation processing is carried out to liquid product, to obtain hydraulic oil product of different viscosities；If feedstock oil uses white oil feedstock oil, the low lime set pressure oil of output, if feedstock oil uses sweat oil, output Group III base oil.
Description
Technical field
The present invention relates to hydraulic oil production technical field more particularly to a kind of production methods of hydraulic oil.
Background technique
Hydraulic oil is exactly the hydraulic medium used using the hydraulic system of liquid pressure energy, and energy is played in hydraulic system
The effects of transmitting, wear-resistant, system lubrication, anti-corrosion, antirust, cooling.For hydraulic oil, hydraulic device should be met first in work
At a temperature of work under start-up temperature to the requirement of liquid viscosity, due to lubricating oil viscosity variation directly with hydraulic operation, transmitting
Efficiency is related with transmitting accuracy, also requires the viscosity temperature characteristic of oil and shear stability that should meet the various need that different purposes are proposed
It asks.
With the development of aircraft industry, hydraulic oil is also widely used in aircraft industry, and aircraft fluid is by naphthenic base crude oil of low-coagulation
The base oil refined through air-distillation, dewaxing by molecular sieve is added made of the modulation such as viscosity index improver, antioxidant, coloring agent
Hydraulic oil has fabulous cryogenic property.The hydraulic oil that plane hydraulic system uses earliest is petroleum base hydraulic oil, due to this
Oil product use has limitation, and the U.S. has developed synthesis hydrocarbon fire resistant hydraulic oil, and the aircraft fluid in China includes stone at present
Oil base and synthetic hydrocarbon oil, while the independent research that succeeded goes out petroleum base hydraulic oil 10, is widely used in military aircraft, China
What aircarrier aircraft mainly used is the phosphate ester hydraulic fluid of import at present, with the development of science and technology, independent research goes out to be used to fly
The high Performance Hydraulic Fluids of machine hydraulic system are the targets that people pursue always, and aviation is to need currently on the market with low lime set pressure oil
A kind of biggish hydraulic oil of the amount of asking.
In addition, to adapt to the rapid development and stringent environmental requirement of automobile, mechanical industry, lube product upgrading
Speed is obviously accelerated, and II/III class base oil demand of HDF of lubricating oil production is continuously increased, according to statistics II/III class basis
The ratio of the world You Zhan market of base oil rises to 23% in 2001 by the 11% of nineteen ninety-five.Global II/ in 2008
Group III oil production capacity is up to 16,000,000 tons or so, accounts for the 30% of aggregated capacity.It is about to Lube Oil In The World demand in 2013
39200000 tons, for III class base oil by under the form for maintaining high demand always, prospect is considerable in the time afterwards.Point
Product quality indicator is analysed, III class base oil probably refers to that saturated hydrocarbon content is greater than or equal to 90%, and sulfur content is less than or equal to
0.03%, viscosity index (VI) is greater than 120 oil product.Its product has very superior performance, such as low viscosity, low volatility, superior
Cold starting performance (superior low temperature flow), good anti-oxidative stability.
Isomerization dewaxing be wax molecule occur isomerization reaction without crack so that wax is changed into ideal composition, this method obtains
Base oil pour point it is low, Viscosity Index is high, and base oil yield is higher than CATALYTIC DEWAXING TECHNIQUE.Isomerization dewaxing catalyst requires
It is difunctional, i.e. strong metal function and the acid function to balance each other with metal function.Ideal isomerization dewaxing catalyst is only catalyzed alkane
Isomerization can be greatly lowered pour point and improve Viscosity Index, only change the chemical structure of alkane, do not destroy bulk of molecule.
But in fact, the acidic components of isomerization dewaxing catalyst always have some cracking activities, there is presently no urging for complete isomerization
Agent.But the purity of either aviation low lime set pressure oil or Group III base oil, the hydraulic oil of China's autonomous production at present begins
Lower eventually, the hydraulic oil of high-purity is mainly also to rely on import, not yet finds the liquid of a preferable method production high-purity
Pressure oil.
In conclusion a kind of method for how seeking manufacturing high-purity hydraulic oil has become those skilled in the art
The technical problem of urgent need to resolve.
Summary of the invention
The object of the present invention is to provide a kind of production methods of hydraulic oil, to improve the hydraulic oil purity manufactured out.
To achieve the goals above, the present invention provides a kind of production method of hydraulic oil, the method comprising the steps of:
Step S1: feedstock oil is mixed with hydrogen, to form mixed raw material；
Step S2: mixed raw material is carried out to be heated to the first preset temperature；
Step S3: it is carried out the isomerizing reactor equipped with shape-selective heterogeneous catalyst is imported by the mixed raw material of heat temperature raising
Reaction is to obtain primary first-order equation effluent, and the shape-selective heterogeneous catalyst is molecular sieve and the shape-selective isocatalysis of platinum palladium noble metal
The mixture of agent；
Step S4: primary first-order equation effluent progress temperature is adjusted to import after the second preset temperature and is urged containing refining reaction
It is reacted to obtain secondary response effluent in the post-refining reactor of agent, and the refining reaction catalyst is molecular sieve
With the mixture of platinum palladium noble metal post-refining catalyst；
Step S5: carrying out gas liquid separation to secondary response effluent, to obtain recycling hydrogen and liquid product；
Step S6: carrying out fractionation processing to liquid product, obtains hydraulic oil product of different motion viscosity；
Wherein, the feedstock oil is white oil, and described hydraulic oil product is low lime set pressure oil；It or is the feedstock oil
For sweat oil, described hydraulic oil product is Group III base oil.
Preferably, the molecular sieve and the shape-selective heterogeneous catalyst of platinum palladium noble metal for including in the shape-selective heterogeneous catalyst
Weight proportion be platinum noble metals accounting 0.35%, palladium noble metal accounting 0.5%, remaining be molecular sieve.
Preferably, the model EM-7611 platinum that the shape-selective heterogeneous catalyst of platinum palladium noble metal is produced by Exxon Mobil
The shape-selective heterogeneous catalyst of model EM-7663 platinum palladium noble metal of the shape-selective heterogeneous catalyst of palladium noble metal and Exxon Mobil production
Composition.
Preferably, the model EM-7611 shape-selective heterogeneous catalyst of platinum palladium noble metal of Exxon Mobil production with angstrom
The weight proportion of the shape-selective heterogeneous catalyst of model EM-7663 platinum palladium noble metal of gram gloomy Mobil production are as follows: 1 to 7.84.
Preferably, the platinum palladium noble metal post-refining catalyst is the ICR419 platinum palladium of Chevron lomars company production
Noble metal post-refining catalyst.
Preferably, first preset temperature is 340 DEG C ± 1 DEG C, and second preset temperature is 240 DEG C ± 1 DEG C.
Preferably, the fractionation processing in the step S6, specifically includes sub-step:
Step S61: liquid product importing atmospheric pressure kiln is warming up to third preset temperature；
Step S62: will heat up to the liquid product of third preset temperature and import the primary fractionation processing of atmospheric fractional tower progress,
Obtain pure white oil plant and primary fractionation residue；
Step S63: it will once be fractionated residue and import vacuum tower, vacuum tower depressurizes the primary fractionation residue
To the first preset pressure and it is warming up to the 4th preset temperature；
Step S64: secondary fractionation processing, institute are carried out by vacuum fractionation tower is imported by the primary fractionation residue of vacuum tower
It states and is disposed with multiple fractionating columns on vacuum fractionation tower from top to bottom, pass through different fractionating column output different motion viscosity
Hydraulic oil；
Step S65: the fractionating column for exporting the hydraulic oil of corresponding kinematic viscosity is connect with steam stripping at reduced pressure tower, by depressurizing vapour
Stripper carries out rectification process, to obtain the hydraulic oil of required purity.
Preferably, the regular precise distillation filler of ripple, the regular accurate essence of the ripple are provided in the steam stripping at reduced pressure tower
It is more abundant for contacting the overheat stripped vapor imported in the steam stripping at reduced pressure tower with hydraulic oil to evaporate filler.
Preferably, the is provided on the fractionating column of the hydraulic oil for importing corresponding kinematic viscosity to the steam stripping at reduced pressure tower
One flow regulator is provided with second flow adjusting for being imported on the pipeline for overheating stripped vapor to the steam stripping at reduced pressure tower
Device.
Content is introduced compared to background technique, the production method of above-mentioned hydraulic oil mixes feedstock oil with hydrogen, to be formed
Mixed raw material；Then mixed raw material is carried out being heated to the first preset temperature；It will be led by the mixed raw material of heat temperature raising
Enter the isomerizing reactor equipped with shape-selective heterogeneous catalyst to be reacted to obtain primary first-order equation effluent, and shape-selective heterogeneous catalyst
For the mixture of molecular sieve and the shape-selective heterogeneous catalyst of platinum palladium noble metal；Primary first-order equation effluent progress temperature is adjusted to second
It is imported in the post-refining reactor containing refining reaction catalyst after preset temperature and is reacted to obtain secondary response effluent,
And refining reaction catalyst is the mixture of molecular sieve and platinum palladium noble metal post-refining catalyst；To secondary response effluent into
Row gas liquid separation, to obtain recycling hydrogen and liquid product；Fractionation processing is carried out to liquid product, to obtain different viscosities
Hydraulic oil product, and when feedstock oil is white oil, it can be with the low lime set pressure oil of output；When feedstock oil is sweat oil, can produce
Group III base oil out.The production method, by the way that shape-selective heterogeneous catalyst is designed to molecular sieve and the shape-selective isomery of platinum palladium noble metal
The mixture of catalyst, refining reaction Catalyst Design at molecular sieve and platinum palladium noble metal post-refining catalyst mixture,
So that hydroisomerizing reaction and hydrofining reaction are more abundant, aphthenic acids, fragrance in oil product are then greatly reduced
The content of the harmful substances such as hydrocarbon, colloid, asphalitine, and can be by the molecular isomerism reaction depth of control oil product, significantly
The pour point of oil product is reduced, and then improves the hydraulic oil purity manufactured out.
Detailed description of the invention
Fig. 1 is the flow sheet that white oil feedstock oil provided in an embodiment of the present invention produces low lime set pressure oil；
Fig. 2 is the flow sheet that sweat oil feedstock oil provided in an embodiment of the present invention produces Group III base oil.
Specific embodiment
Core of the invention is to provide a kind of production method of hydraulic oil, to improve the hydraulic oil purity manufactured out.
In order to make those skilled in the art more fully understand technical solution provided by the invention, below in conjunction with attached drawing and
The present invention is described in further detail for specific embodiment.
As depicted in figs. 1 and 2, the production method of a kind of hydraulic oil provided in an embodiment of the present invention, the method comprising the steps of:
Step S1: feedstock oil is mixed with hydrogen, to form mixed raw material, specifically can be and feedstock oil is passed through feedstock oil
Surge tank, then accesses new hydrogen pipeline on the outgoing line of feedstock oil surge tank, and certain those skilled in the art should
, it is understood that new hydrogen pipeline needs logical in order to guarantee that hydrogen can smoothly import the outgoing line of feedstock oil surge tank
Overcompression machine pressurizes；
Step S2: mixed raw material is carried out to be heated to the first preset temperature, it should be noted that the first default temperature
Degree is generally located on 340 DEG C ± 1 DEG C, because when experiment shows to produce Group III base oil using sweat oil, most preferred temperature
It is 340 DEG C；When for producing low lime set pressure oil, effect when the first preset temperature is arranged to 330 DEG C is optimal, is most suitable for this hair
The reaction temperature of isomerizing reactor in bright, it is of course possible to which understanding, the temperature value are only the embodiment of the present invention for excellent
Select the citing of temperature, in actual application, can also be selected according to the required temperature of isomerizing reactor it is corresponding other
Temperature value；
Step S3: it is carried out the isomerizing reactor equipped with shape-selective heterogeneous catalyst is imported by the mixed raw material of heat temperature raising
Reaction is to obtain primary first-order equation effluent, and shape-selective heterogeneous catalyst is molecular sieve and the shape-selective heterogeneous catalyst of platinum palladium noble metal
Mixture；
Step S4: primary first-order equation effluent progress temperature is adjusted to import after the second preset temperature and is urged containing refining reaction
It is reacted to obtain secondary response effluent in the post-refining reactor of agent, and refining reaction catalyst is molecular sieve and platinum
The mixture of palladium noble metal post-refining catalyst, it should be noted that in general, which is preferably 240
DEG C ± 1 DEG C, because when experiment is shown for producing low lime set pressure oil, effect when the second preset temperature is arranged to 240 DEG C is most
It is excellent, it is most suitable for the reaction temperature of the post-refining reactor in the present invention, it is of course possible to which understanding, the temperature value are only this
Citing of the inventive embodiments for preferable temperature can also be according to the institute of post-refining reactor in actual application
Temperature is needed to select other corresponding temperature values；
Step S5: gas liquid separation is carried out to secondary response effluent, to obtain recycling hydrogen and liquid product, is needed
It is bright, in order to enable hydrogen can recycle, feedstock oil is accessed again after generally recycling hydrogen is pressurizeed by compressor
On the outgoing line of surge tank, for example access amount can be 33000Nm3/ h can substantially reduce the consumption of new hydrogen in this way,
To a certain extent being capable of save the cost, naturally it is also possible to be recycled in returnable bottle it is stand-by, in addition, the side of gas liquid separation processing
Formula generally successively passes through high-pressure separator and low pressure separator, after exporting high score oil by high-pressure separator, enters back into low pressure
Separator exports low point of oil, continues step S6 after entering later；
Step S6: carrying out fractionation processing to liquid product, to obtain different grades of hydraulic oil product；
It wherein, can be with the low lime set pressure oil of output when feedstock oil is white oil；It, can be with output when feedstock oil is sweat oil
Group III base oil.
The production method, by the way that shape-selective heterogeneous catalyst is designed to molecular sieve and the shape-selective heterogeneous catalyst of platinum palladium noble metal
Mixture, refining reaction Catalyst Design at molecular sieve and platinum palladium noble metal post-refining catalyst mixture so that plus
Hydrogen isomerization reaction and hydrofining reaction are more abundant, then greatly reduce aphthenic acids, aromatic hydrocarbon, glue in oil product
The content of the harmful substances such as matter, asphalitine, and can be greatly reduced by the molecular isomerism reaction depth of control oil product
The pour point of oil product, and then improve the purity for the hydraulic oil manufactured out.
In some more specifical embodiments, the molecular sieve and the expensive gold of platinum palladium that include in above-mentioned shape-selective heterogeneous catalyst
Belong to shape-selective heterogeneous catalyst weight proportion be platinum noble metals accounting 0.35%, palladium noble metal accounting 0.5%, remaining be molecule
Sieve, it is of course possible to which understanding, above-mentioned weight proportion are only the preferable examples of the embodiment of the present invention, actual application
In, it can also be that, according to real reaction demand, selection is designed to the form of other weight proportions.
In other specific embodiment, the molecular sieve and platinum palladium noble metal for including in refining reaction catalyst are mended
Fill catalyst for refining weight proportion be platinum noble metals accounting 0.35%, palladium noble metal accounting 0.5%, remaining be molecular sieve, when
So it is understood that above-mentioned weight proportion is only the preferable examples of the embodiment of the present invention, in actual application, also
It can be according to real reaction demand, selection is designed to the form of other weight proportions.
It should be noted that in general, the model that the shape-selective heterogeneous catalyst of platinum palladium noble metal is produced by Exxon Mobil
The model EM-7663 platinum palladium noble metal produced for the shape-selective heterogeneous catalyst of EM-7611 platinum palladium noble metal and Exxon Mobil is selected
Shape heterogeneous catalyst composition.Also, in general, it is preferred to which the model EM-7611 platinum palladium noble metal of Exxon Mobil production is selected
The weight proportion of shape heterogeneous catalyst and the shape-selective heterogeneous catalyst of model EM-7663 platinum palladium noble metal of Exxon Mobil production
Are as follows: 1 to 7.84.Of course, it should be understood that above-mentioned weight proportion is only the preferable examples of the embodiment of the present invention, it is practical
In application process, it can also be that, according to real reaction demand, selection is designed to the form of other weight proportions.
It is further to note that platinum palladium noble metal post-refining catalyst is generally preferred to the life of Chevron lomars company
The ICR419 platinum palladium noble metal post-refining catalyst of production.It is selected because the present invention attempts discovery by test in platinum palladium noble metal
The shape-selective heterogeneous catalyst of model EM-7611 platinum palladium noble metal and Exxon beauty that shape heterogeneous catalyst is produced by Exxon Mobil
When inspiring confidence in the model EM-7663 platinum palladium noble metal shape-selective heterogeneous catalyst composition of production, the production of Chevron lomars company is selected
ICR419 platinum palladium noble metal post-refining catalyst easily facilitate control isomerization reaction depth, what be will be understood
It is the catalyst that can also be other other producers productions with same effect well-known to those skilled in the art, only not
It crosses in the application preferably using the ICR419 platinum palladium noble metal post-refining catalyst of Chevron lomars company production.
Moreover, it is desirable to illustrate, the fractionation processing in step S6 can specifically include following sub-step:
Step S61: the liquid product of secondary response outflow is imported into atmospheric pressure kiln and is warming up to third preset temperature, the third is pre-
If temperature is generally located on 320 DEG C ± 2 DEG C；
Step S62: will heat up to the liquid product of third preset temperature and import the primary fractionation processing of atmospheric fractional tower progress,
By being once fractionated the available pure white oil plant of processing and primary fractionation residue；
Step S63: will once be fractionated residue and import vacuum tower, and vacuum tower be decompressed to the to primary fractionation residue
One preset pressure is simultaneously warming up to the 4th preset temperature, which is traditionally arranged to be 4KPa, the 4th preset temperature one
As be arranged at 350 DEG C ± 2 DEG C；
Step S64: secondary fractionation processing is carried out by vacuum fractionation tower is imported by the primary fractionation residue of vacuum tower, is subtracted
Multiple fractionating columns are disposed on pressure fractionating tower from top to bottom, pass through the hydraulic of different fractionating column output different motion viscosity
Oil, if feedstock oil, using white oil feedstock oil, vacuum fractionation tower can be disposed with first point from top to bottom at this time
Evaporate pipe, after-fractionating pipe, third fractionating column, the 4th fractionating column and the 5th fractionating column；After secondary fractionation processing, the first fractionating column
Pure white oil plant is exported, after-fractionating pipe exports No. 5 white oils, and the 5th fractionating column exports No. 100 white oils, third fractionating column and the 4th point
It evaporates pipe and carries out No. 10 white oils of rectification process output and No. 32 white oils for accessing steam stripping at reduced pressure tower；If feedstock oil is using under wax
Oil, final product be obtain Group III base oil, at this time vacuum fractionation tower can be disposed with from top to bottom the first fractionating column,
After-fractionating pipe, third fractionating column, the 4th fractionating column, the 5th fractionating column and the 6th fractionating column；After secondary fractionation processing, first
Fractionating column exports pure white oil plant, and after-fractionating pipe exports the white oil of 60N, is the white oil of 500N, third derived from the 6th fractionating column
Fractionating column, the 4th fractionating column and the 5th fractionating column access steam stripping at reduced pressure tower and carry out rectification process, final corresponding output 150N,
The white oil of 250N, 350N；
Step S65: the fractionating column for exporting the hydraulic oil of corresponding kinematic viscosity is connect with steam stripping at reduced pressure tower, by depressurizing vapour
Stripper carries out rectification process, to obtain the hydraulic oil of required purity.
Above-mentioned fractionation processing combines the form of rectification process due to using second level fractionation so that processing and fabricating go out it is low solidifying
The purity of hydraulic oil is higher, more high-quality.Of course, it should be understood that the above-mentioned form for combining rectification process using second level fractionation
The only preferable examples of the embodiment of the present invention, in actual application, more good hydraulic oil, can also be selected in order to obtain
Select the form for being arranged to three-level fractionation cooperation rectification process or three-level or more fractionation cooperation rectification process.
In some more specifical embodiments, in order to further enhance the treatment effect of rectification process, in decompression vapour
The regular precise distillation filler of ripple is additionally provided in stripper, the regular precise distillation filler of ripple imports in steam stripping at reduced pressure tower for making
The overheat stripped vapor temperature of stripped vapor (overheat be generally 400 DEG C -420 DEG C) contacted with hydraulic oil it is more abundant.It needs
Illustrate, in general, is located at ripple rule for importing the import of pipeline of overheat stripped vapor to the steam stripping at reduced pressure tower
The lower section of whole precise distillation filler, the import position of the fractionating column of the hydraulic oil for importing corresponding kinematic viscosity to steam stripping at reduced pressure tower
In the regular precise distillation filler face of ripple or position on the upper side.Using existing steam stripping at reduced pressure tower, in vacuum 1st side cut stripper
One section of corrugated regular filler of interior increase isolates narrow component to improve the rectification effect of vacuum 1st side cut product, can then obtain
Low condensation point 15# aircraft fluid.
In order to guarantee the safety and stability of entire process flow operation, for importing to steam stripping at reduced pressure tower to meeting the tendency of
It is provided with first flow regulating device on the fractionating column of the hydraulic oil of kinetic viscosity, can effectively be controlled by first flow regulating device
Flow of the big tower of vacuum 1st side cut processed into steam stripping at reduced pressure tower, it is ensured that qualified product；For importing hot vapour to steam stripping at reduced pressure tower
It mentions and is provided with second flow regulating device on the pipeline of steam, it can be to avoid the hair for rushing tower accident by second flow regulating device
It is raw.It should be noted that the specific constructive form of first flow regulating device and second flow regulating device, can be flow tune
Valve or restriction orifice are saved, or is other common flow adjusting structures of those skilled in the art.
The production method of hydraulic oil provided by the present invention is described in detail above.It should be noted that this theory
Various embodiments are described in a progressive manner in bright book, the highlights of each of the examples are with other embodiments
Difference, the same or similar parts between the embodiments can be referred to each other.
It should also be noted that, herein, such as the terms "include", "comprise" or its any other variant are intended to contain
Lid non-exclusive inclusion, so that article or equipment including a series of elements not only include those elements, but also
It including other elements that are not explicitly listed, or further include for this article or the intrinsic element of equipment.Do not having
In the case where more limitations, the element that is limited by sentence "including a ...", it is not excluded that in the article including above-mentioned element
Or there is also other identical elements in equipment.
Used herein a specific example illustrates the principle and implementation of the invention, and above embodiments are said
It is bright to be merely used to help understand the core idea of the present invention.It should be pointed out that for those skilled in the art,
Without departing from the principle of the present invention, can be with several improvements and modifications are made to the present invention, these improvement and modification
It falls into the protection scope of the claims in the present invention.
Claims (9)
1. a kind of production method of hydraulic oil, which is characterized in that the method comprising the steps of:
Step S1: feedstock oil is mixed with hydrogen, to form mixed raw material；
Step S2: mixed raw material is carried out to be heated to the first preset temperature；
Step S3: it is reacted the isomerizing reactor equipped with shape-selective heterogeneous catalyst is imported by the mixed raw material of heat temperature raising
To obtain primary first-order equation effluent, and the shape-selective heterogeneous catalyst is molecular sieve and the shape-selective heterogeneous catalyst of platinum palladium noble metal
Mixture；
Step S4: primary first-order equation effluent progress temperature is adjusted to import after the second preset temperature and contains refining reaction catalyst
Post-refining reactor in reacted to obtain secondary response effluent, and the refining reaction catalyst is molecular sieve and platinum
The mixture of palladium noble metal post-refining catalyst；
Step S5: carrying out gas liquid separation to secondary response effluent, to obtain recycling hydrogen and liquid product；
Step S6: carrying out fractionation processing to liquid product, to obtain hydraulic oil product of different motion viscosity；
Wherein, the feedstock oil is white oil, and described hydraulic oil product is low lime set pressure oil；It or is that the feedstock oil is wax
Lower oil, described hydraulic oil product are Group III base oil.
2. the production method of hydraulic oil as described in claim 1, which is characterized in that include in the shape-selective heterogeneous catalyst
The weight proportion of molecular sieve and the shape-selective heterogeneous catalyst of platinum palladium noble metal is platinum noble metals accounting 0.35%, palladium noble metal accounts for
Than 0.5%, remaining be molecular sieve.
3. the production method of hydraulic oil as claimed in any one of claims 1-3, which is characterized in that the platinum palladium noble metal is selected
The shape-selective heterogeneous catalyst of model EM-7611 platinum palladium noble metal and Exxon beauty that shape heterogeneous catalyst is produced by Exxon Mobil
Inspire confidence in the shape-selective heterogeneous catalyst composition of model EM-7663 platinum palladium noble metal of production.
4. the production method of hydraulic oil as claimed in claim 4, which is characterized in that the model of the Exxon Mobil production
The EM-7611 shape-selective heterogeneous catalyst of platinum palladium noble metal and the model EM-7663 platinum palladium noble metal that Exxon Mobil produces are shape-selective
The weight proportion of heterogeneous catalyst are as follows: 1 to 7.84.
5. the production method of hydraulic oil as claimed in any one of claims 1-3, which is characterized in that the platinum palladium noble metal is mended
Fill the ICR419 platinum palladium noble metal post-refining catalyst that catalyst for refining is the production of Chevron lomars company.
6. the production method of hydraulic oil as described in claim 1, which is characterized in that first preset temperature is 340 DEG C ± 1
DEG C, second preset temperature is 240 DEG C ± 1 DEG C.
7. the production method of hydraulic oil as described in claim 1, which is characterized in that the fractionation processing in the step S6, tool
Body includes sub-step:
Step S61: liquid product importing atmospheric pressure kiln is warming up to third preset temperature；
Step S62: it will heat up to the liquid product of third preset temperature and import the primary fractionation processing of atmospheric fractional tower progress, obtain
Pure white oil plant and primary fractionation residue；
Step S63: will once be fractionated residue and import vacuum tower, and vacuum tower be decompressed to the to the primary fractionation residue
One preset pressure is simultaneously warming up to the 4th preset temperature；
Step S64: carrying out secondary fractionation processing for vacuum fractionation tower is imported by the primary fractionation residue of vacuum tower, described to subtract
Multiple fractionating columns are disposed on pressure fractionating tower from top to bottom, pass through the hydraulic of different fractionating column output different motion viscosity
Oil；
Step S65: the fractionating column for exporting the hydraulic oil of corresponding kinematic viscosity is connect with steam stripping at reduced pressure tower, passes through steam stripping at reduced pressure tower
Rectification process is carried out, to obtain the hydraulic oil of required purity.
8. the production method of hydraulic oil as claimed in claim 8, which is characterized in that be provided with ripple in the steam stripping at reduced pressure tower
Regular precise distillation filler, the regular precise distillation filler of ripple are used for the mistake thermal stripping for making to import in the steam stripping at reduced pressure tower
Steam contacts more abundant with hydraulic oil.
9. the production method of hydraulic oil as claimed in claim 8 or 9, which is characterized in that for being led to the steam stripping at reduced pressure tower
Enter and be provided with first flow regulating device on the fractionating column of the hydraulic oil of corresponding kinematic viscosity, for being led to the steam stripping at reduced pressure tower
Enter to overheat and is provided with second flow regulating device on the pipeline of stripped vapor.
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| CN110272761A (en) * | 2019-07-29 | 2019-09-24 | 海南汉地阳光石油化工有限公司 | A kind of production method and process units of easer |
| CN110317639A (en) * | 2019-07-29 | 2019-10-11 | 海南汉地阳光石油化工有限公司 | A kind of processing technology and processing unit (plant) of conduction oil |
| CN112899025A (en) * | 2021-02-25 | 2021-06-04 | 海南汉地阳光石油化工有限公司 | Preparation method of green food-grade white oil special for dust inhibitor |
| CN114874810A (en) * | 2022-04-28 | 2022-08-09 | 海南汉地阳光石油化工有限公司 | 60N white oil agent for artificial fibers and preparation method thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101514294A (en) * | 2009-03-31 | 2009-08-26 | 中国石油化工集团公司 | Method for reducing aviation kerosene corrosion |
| CN102471704A (en) * | 2009-08-18 | 2012-05-23 | 吉坤日矿日石能源株式会社 | Method for producing lubricant base oil |
| CN107987883A (en) * | 2017-11-23 | 2018-05-04 | 海南汉地阳光石油化工有限公司 | A kind of shape-selective isomery-supplementing refining method of WSI high-pressure hydrogenations |
| CN109181768A (en) * | 2018-09-26 | 2019-01-11 | 海南汉地阳光石油化工有限公司 | A kind of preparation method of low temp area motor-car transmission oil |
| CN109181767A (en) * | 2018-09-26 | 2019-01-11 | 海南汉地阳光石油化工有限公司 | A kind of preparation method of high speed engine base oil |
-
2019
- 2019-01-28 CN CN201910083029.3A patent/CN109722304A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101514294A (en) * | 2009-03-31 | 2009-08-26 | 中国石油化工集团公司 | Method for reducing aviation kerosene corrosion |
| CN102471704A (en) * | 2009-08-18 | 2012-05-23 | 吉坤日矿日石能源株式会社 | Method for producing lubricant base oil |
| CN107987883A (en) * | 2017-11-23 | 2018-05-04 | 海南汉地阳光石油化工有限公司 | A kind of shape-selective isomery-supplementing refining method of WSI high-pressure hydrogenations |
| CN109181768A (en) * | 2018-09-26 | 2019-01-11 | 海南汉地阳光石油化工有限公司 | A kind of preparation method of low temp area motor-car transmission oil |
| CN109181767A (en) * | 2018-09-26 | 2019-01-11 | 海南汉地阳光石油化工有限公司 | A kind of preparation method of high speed engine base oil |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110272761A (en) * | 2019-07-29 | 2019-09-24 | 海南汉地阳光石油化工有限公司 | A kind of production method and process units of easer |
| CN110317639A (en) * | 2019-07-29 | 2019-10-11 | 海南汉地阳光石油化工有限公司 | A kind of processing technology and processing unit (plant) of conduction oil |
| CN112899025A (en) * | 2021-02-25 | 2021-06-04 | 海南汉地阳光石油化工有限公司 | Preparation method of green food-grade white oil special for dust inhibitor |
| CN114874810A (en) * | 2022-04-28 | 2022-08-09 | 海南汉地阳光石油化工有限公司 | 60N white oil agent for artificial fibers and preparation method thereof |
| CN114874810B (en) * | 2022-04-28 | 2024-04-12 | 海南汉地阳光石油化工有限公司 | 60N white oil agent for artificial fiber and preparation method thereof |
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