CN107400535A - A kind of method and isoparaffin solvent oil of F- T synthesis naphtha production isoparaffin solvent oil - Google Patents
A kind of method and isoparaffin solvent oil of F- T synthesis naphtha production isoparaffin solvent oil Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
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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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
- C10G69/126—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step polymerisation, e.g. oligomerisation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
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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
- C10G2400/18—Solvents
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Abstract
The present invention relates to Fischer-Tropsch synthesis oil production isoparaffin solvent oil field, discloses a kind of method and isoparaffin solvent oil of F- T synthesis naphtha production isoparaffin solvent oil.This method includes：(1) F- T synthesis naphtha is subjected to alcohol halogenating reaction to convert alcohol as halogenated alkane；(2) product that step (1) obtains is subjected to polymerisation in the presence of polymerization catalyst；(3) product that step (2) obtains is subjected to hydrogenation reaction in the presence of a hydrogenation catalyst；(4) initial boiling point is not less than 160 DEG C in the product of collection step (3) and the end point of distillation is not more than 340 DEG C of cut.By the method for the present invention, the yield and purity of obtained isoparaffin solvent oil are high, and the of light color of isoparaffin solvent oil product, oxidation stability and heat endurance are good, and the content of aromatic hydrocarbons, sulphur and nitrogen compound can be neglected.
Description
Technical field
The present invention relates to isoparaffin solvent oil field, in particular it relates to a kind of isoparaffin solvent oil and
The method that F- T synthesis naphtha produces isoparaffin solvent oil
Background technology
Solvent oil product is one of five major class oil products.Solvent oil product can be divided into aromatic hydrocarbon, Porous deproteinized bone
Aliphatic category, isomeric alkane hydro carbons, cycloalkane and n-alkane etc..
Normal alkane solvent oil has relatively low viscosity, and the n-alkane of several grades is sold by Exxon companies
Solvent naphtha NORPAR solvents, almost completely by C10-C15Linear paraffin is formed, but they also have phase
When high pour point.
Isoparaffin solvent oil has the characteristics that condensation point is low, smell is small, toxicity is low and good security.Exxon
ISOPAR solvent naphthas (the C of several grades sells in company5-C20), paraffins mixture structure is branched by height
Into having low-down normal paraffin content.They have fabulous cryogenic property, are widely used in printing
Contaminate diluent, printing ink solvent, intermetallic composite coating cleaning agent, antirust oil, tasteless spray, tasteless oil paint,
Paint, organosol formula, advanced clothes dry cleaner's naphtha, peroxide organic compound supporting agent, washing daily use chemicals production
Product etc..
The production of isoparaffin solvent oil at present passes through alkyl mainly using isoparaffin and alkene as raw material
Change reaction, hydrogenated redistillation obtains isoparaffin solvent oil.This method is commonly available gasoline fraction
The isoparaffin solvent oil of scope, but produce kerosene or the isoparaffin solvent oil of diesel oil distillate scope
(150~350 DEG C) are more difficult.
Fischer-Tropsch synthesis oil have the undesirable components content such as sulphur, nitrogen, aromatic hydrocarbons it is extremely low, it is main composition be chain type
The features such as hydrocarbon, cycloalkane and seldom arene content.Existing method is passed through using F- T synthesis light fraction oil
Hydro-upgrading directly obtains solvent naphtha.The solvent naphtha has high selection dissolubility, high stability, colourless nothing
The features such as taste, low-viscosity, but product is almost made up of n-alkane completely, has higher condensation point.For
This needs to improve isoparaffin content using hydrofinishing-hydroisomerizing joint processing scheme.
US5,866,748, which discloses to use, contains C8~C20The predominantly raw material of n-alkane, such as Fischer-Tropsch synthesis oil,
The method that isoparaffin content is more than 50% solvent naphtha is prepared by hydroisomerizing, the solvent naphtha of preparation
Cryogenic property and viscosity are obviously improved.Fischer-Tropsch synthesis oil in other this method is low olefin component
Content.
In Fischer-Tropsch synthesis oil, cut is lighter, and the olefin(e) centent in oil product is higher, and Determination of Alkane Content is lower.Take
Olefin(e) centent highest in support synthesis light fraction oily (abbreviation Fischer-Tropsch light fraction), olefin(e) centent can be with
Reach more than 40 weight %.Therefore the high Fischer-Tropsch light fraction of other technologies processing olefin(e) centent is needed.
US6,605,206B1 discloses a kind of C of the increase from F- T synthesis10The receipts of above hydrocarbon products
The method of rate, it includes：(a) C will be contained5The feed separation of above Fischer-Tropsch synthetic is Fischer-Tropsch wax
With Fischer-Tropsch liquids cut (being referred to as condensate fraction, wherein being less than 400 DEG C of alcohol containing boiling point)；(b) will take
It is higher boiling, the medium than Fischer-Tropsch wax more low pour point to hold in the palm wax catalytic dewaxing；(c) hydrofinishing higher boiling is situated between
Matter；(d) Fischer-Tropsch condensate fraction isolated in step (a) is contacted with dealcoholysis catalyst, make to
Alcohol in small part cut is changed into alkene；(e) olefin(e) oligomerization in Fischer-Tropsch condensate fraction is formed into medium
Oligomer mixture, there is the mean molecule quantity higher than Fischer-Tropsch condensate fraction；(f) medium oligomerisation is mixed
Compound hydrofinishing；And (g) recovery obtains C10Above hydrocarbon products.This method can produce lubrication
Oil base oil, and diesel product.
US2,004,267,071A1 discloses a kind of by the Fischer-Tropsch conjunction containing alkene and hopcalite
The oxide in Fischer-Tropsch light fraction oil is reduced into the method for condensate oligomerisation, including (a), (b) exists
The product of step (a) is in contact with ionic-liquid catalyst under the conditions of oligomerisation reaction, and (c) is returned
Charge support synthesis of derivatives product, has the mean molecule quantity higher compared to F- T synthesis condensate and increase
The degree of branching molecule, can obtain diesel oil and lubricating oil component by hydrofinishing.
CN104560193A discloses a kind of preparation method of lube base oil and/or solvent naphtha, bag
Include：(1) polymerisation, the polymer raw bag occur in the presence of Lewis acid catalysts for polymer raw
Olefin-containing, alcohol and non-essential alkane, in the polymer raw olefin(e) centent more than 10 mass %,
The oxygen content provided by alcohol is 0.2%~2%；On the basis of the alkene, alpha-olefin in the alkene
Content >=85%；The mass ratio of the Lewis acid catalysts and alkene in polymer raw is 1：(200~5),
The mass ratio of the Lewis acid catalysts and oxygen element in polymer raw is (2~70)：1；(2) step
Suddenly hydrofinishing and/or hydroisomerizing reaction further occur for the polymerizate of (1)；(3) collection step
(2) cut of the initial boiling point more than 340 DEG C obtains lube base oil and/or the end point of distillation in reaction product
Cut less than 340 DEG C obtains solvent naphtha.But this method is high to ingredient requirement alpha-olefin content, with suitable
In obtaining lube base oil, it is few to obtain solvent naphtha still isoparaffin content.
Contain a certain amount of organic oxygen-containing compound, mainly alcohol in FT artificial oils.The organic oxygen-containings such as alcohol
Compound can be complexed to be formed as the Lewis acid catalysts of proton donor type co-catalyst and polymerisation
Complex ions pair with catalytic activity, but when the organic oxygen-containing compound excess such as alcohol, Lewis
Acid catalyst can poison inactivation by organic oxygen-containing compounds such as alcohol.
In Fischer-Tropsch synthesis oil, especially alkene in F- T synthesis naphtha (end point of distillation be not more than 160 DEG C)
Hydrocarbon content is higher, how to process Fischer-Tropsch synthetic naphtha, and the isoparaffin for obtaining kerosene and diesel oil distillate is molten
Agent oil, and wherein isoparaffin content height is, it is necessary to explore new suitable method.
The content of the invention
The invention aims to solve how to process to obtain isoparaffin by F- T synthesis naphtha to contain
The problem of measuring high isoparaffin solvent oil, there is provided a kind of F- T synthesis naphtha production isoparaffin is molten
The method and isoparaffin solvent oil of agent oil.Wherein, after F- T synthesis naphtha first carries out alcohol halogenating reaction
Carry out the polymerisation of alkene again and can reduce to be poisoned inactivation for the Lewis acid catalysts of polymerisation
Possibility, it is possible thereby to reduce polymerization catalyst dosage or increase isoparaffin solvent oil yield.
The present inventor has found in surprise under study for action, using F- T synthesis naphtha as raw material, by Fischer-Tropsch
Synthetic naphtha carries out alcohol halogenating reaction, polymerisation and hydrogenation reaction successively, and preferably control is specific
Polymeric reaction condition can obtain more dimerisation products, can obtain yield and isoparaffin purity is bright
Aobvious higher isoparaffin solvent oil.
Therefore, to achieve these goals, in a first aspect, the invention provides a kind of F- T synthesis stone brain
The method of oil production isoparaffin solvent oil, including：
(1) F- T synthesis naphtha is subjected to alcohol halogenating reaction under catalyst action, makes F- T synthesis
Alcohol in naphtha is converted into halogenated alkane；
(2) product that step (1) obtains is subjected to polymerisation in the presence of polymerization catalyst, makes step
Suddenly the alkene in the product that (1) obtains is converted into target product as the poly- of dimerization compound and/or trimerization compound
Close product；
(3) product that step (2) obtains is subjected to hydrogenation reaction in the presence of a hydrogenation catalyst, makes step
Suddenly the polymerizate in the product that (2) obtain is converted into saturated alkane, while the production that step (2) obtains
Halogenated alkane dehalogenate in thing is converted into alkane；
(4) by be fractionated in the product of cutting step (3) initial boiling point not less than 160 DEG C and the end point of distillation not
Cut more than 340 DEG C, obtains isoparaffin solvent oil.
Second aspect, the invention provides the isoparaffin solvent oil obtained by the above method, the isomeric alkane
The boiling range of hydrocarbon solvent oil is 160 DEG C~340 DEG C, wherein, using the gross weight of the isoparaffin solvent oil as base
Standard, the content of isoparaffin is more than 98 weight %；It is preferred that the oxygen content of the isoparaffin solvent oil
For below 0.1 weight %, arene content is below 0.05 volume %.
In the method for the F- T synthesis naphtha production isoparaffin solvent oil of the present invention, Isopars
The high income of oil, can reach more than 80% (yield is on the basis of the alkene in polymerisation raw material)；And
The purity of isoparaffin is high in solvent naphtha, and its content can reach more than 98%.Meanwhile by the inventive method
It is good to produce obtained the of light color of isoparaffin solvent oil product, oxidation stability and heat endurance, aromatic hydrocarbons,
The content of sulphur and nitrogen compound can be neglected.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Embodiment
The embodiment of the present invention is described in detail below.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The end points of disclosed scope and any value are not limited to the accurate scope or value herein, this
A little scopes or value should be understood to comprising the value close to these scopes or value.For number range, respectively
Between the endpoint value of individual scope, between the endpoint value of each scope and single point value, and single point
Can be combined with each other between value and obtain one or more new number ranges, these number ranges should by regarding
For specific disclosure herein.
In a first aspect, the invention provides a kind of side of F- T synthesis naphtha production isoparaffin solvent oil
Method, including：
(1) F- T synthesis naphtha is subjected to alcohol halogenating reaction under catalyst action, makes F- T synthesis
Alcohol in naphtha is converted into halogenated alkane；
(2) product that step (1) obtains is subjected to polymerisation in the presence of polymerization catalyst, makes step
Suddenly the alkene in the product that (1) obtains is converted into target product as the poly- of dimerization compound and/or trimerization compound
Close product；
(3) product that step (2) obtains is subjected to hydrogenation reaction in the presence of a hydrogenation catalyst, makes step
Suddenly the polymerizate in the product that (2) obtain is converted into saturated alkane, while the production that step (2) obtains
Halogenated alkane dehalogenate in thing is converted into alkane；
(4) by be fractionated in the product of cutting step (3) initial boiling point not less than 160 DEG C and the end point of distillation not
Cut more than 340 DEG C, obtains isoparaffin solvent oil.
In the method for the present invention, in order to improve isoparaffin in the yield of isoparaffin solvent oil and solvent naphtha
Purity, under preferable case, F- T synthesis naphtha is the F- T synthesis stone that the end point of distillation is not more than 160 DEG C
Cerebrol raw material, wherein, on the basis of the gross weight of the F- T synthesis naphtha, the F- T synthesis stone
Cerebrol contains alkene more than 20 weight %；On the basis of the gross weight of the alkene, α in the alkene-
The content of alkene is less than 85 weight %.
In the method for the present invention, F- T synthesis naphtha contains alkene, oxygenatedchemicals and alkane, with institute
On the basis of stating F- T synthesis naphtha gross weight, olefin(e) centent is more than 20 weight %, preferably in 30 weights
More than % is measured, further preferably more than 40 weight %；Organic oxygen-containing compound content 1 weight % with
On, preferably more than 5 weight %, further preferably more than 10 weight %；Determination of Alkane Content is in 10 weights
More than % is measured, preferably more than 20 weight %.Wherein, under preferable case, with the F- T synthesis stone brain
On the basis of oily gross weight, olefin(e) centent is 30~80 weight %；Organic oxygen-containing compound content is 1~30
Weight %；Determination of Alkane Content is 20~40 weight %.Wherein, using the F- T synthesis naphtha gross weight as
Benchmark, the alcohol content contained in organic oxygen-containing compound are 1~25 weight %, preferably 10~20 weights
Measure %；The content of n-alkane is 10~40 weight %, preferably 20~30 weight %；Isoparaffin
Content be 0~10 weight %, preferably 0~7 weight %；N-alkanol content is 5~15 weight %,
Preferably 10~15 weight %.Preferably, on the basis of the gross weight of the alkene, α in the alkene-
The content of alkene is 10~84.5 weight %.
In the inventive method, F- T synthesis naphtha can be in F- T synthesis light oil one section evaporate
Journey, the end point of distillation evaporating no more than 160 DEG C can be cut out by the way that F- T synthesis light oil is carried out into rectifying
Divide and obtain.Wherein the composition of F- T synthesis light oil can contain C2~C25Alkane and alkene, with
And the oxygenatedchemicals such as alcohol.The rectifying can be the rectifying mode that this area routinely uses, and can use
Conventional use of rectifying column is implemented.
In the present invention, F- T synthesis light oil comes from Fischer-Tropsch synthesis process, composition can contain alkane,
Alkene and alcohol, the carbon number of these compounds is 2 to 25 or so.Determination of Alkane Content can be 30~35 weight
%, olefin(e) centent can be 40~45 weight %, and alcohol content can be 8~12 weight %, can also contain
It is 9~13 weight % to have other compounds contents.Further, characterized by H-NMR, in alkene
80~95 weight %, the Inner alkene that middle alpha-olefin accounts for total olefin account for 5~20 weight % of total olefin.Fischer-Tropsch closes
Into light oil and with certain boiling range scope compound mixture, preferably the end point of distillation be 360 DEG C.
In the inventive method, the alcohol halogenating reaction can be the alkoxide component in the F- T synthesis naphtha
Reacted with halide, help to convert alcohol, when reducing the polymerisation of progress subsequently, alcohol pair
The negative effect of the polymerisation, mainly there is the inactivation for causing polymerization catalyst, make polymerization catalyst
Dosage increase.Under preferable case, in step (1), alcohol halogenating reaction condition includes：Temperature be 25~
80 DEG C, preferably 30~60 DEG C.By (1) the step of method of the invention, the F- T synthesis is converted
Alkoxide component in naphtha, the dosage of polymerization catalyst can be greatly reduced.
In the inventive method, can be used for the alcohol halogenating reaction halide can be HCl, HBr,
HI, it can correspondingly use the different catalyst for the alcohol halogenating reaction.Under preferable case, step
Suddenly in (1), F- T synthesis naphtha carry out alcohol halogenating reaction catalyst can be anhydrous zinc chloride or
Sulfuric acid.
Preferably, the halide for the alcohol halogenating reaction is HCl, and used catalyst is anhydrous chlorination
Zinc.
It is further preferred that the catalyst that F- T synthesis naphtha carries out alcohol halogenating reaction is to contain anhydrous zinc chloride
Concentrated hydrochloric acid solution.Such as in the concentrated hydrochloric acid solution of the anhydrous zinc chloride anhydrous zinc chloride (with ZnCl2Meter)
Mol ratio with pure concentrated hydrochloric acid (HCl meters) is 1：1.Such as 1mol anhydrous zinc chlorides can be dissolved in
1mol concentrated hydrochloric acids prepare the concentrated hydrochloric acid solution containing anhydrous zinc chloride.
In the present invention, the particularly preferred F- T synthesis naphtha and the concentrated hydrochloric acid containing anhydrous zinc chloride are molten
The volume ratio of liquid is (1.5~2.5)：1, preferably volume ratio is 2.
In the inventive method, above-mentioned alcohol halogenating reaction can reduce shadow of the alcohol to subsequent polymerisation reaction catalyst
Ring.
In the inventive method, after the completion of the alcohol halogenating reaction, the alcohol in F- T synthesis naphtha is converted into
Halogenated alkane.The product of the alcohol halogenating reaction further can be subjected to static layering, alcohol and water
The concentrated hydrochloric acid solution for being dissolved in anhydrous zinc chloride is lower floor, and dense salt of the halogenated alkane insoluble in anhydrous zinc chloride
Acid solution is upper strata, takes upper strata to carry out the reactant of the polymerisation of step (2).
In the inventive method, the present inventor has further been found that in polymerisation mistake under study for action
Low molecular alkene is converted into heavier product in journey, while the carbon backbone structure of polymer is in molecule addition
Side chain is formed at point, passes through the specific reaction temperature for controlling polymerisation and specific reaction time, Neng Gougeng
More generation dimerisation products, trimerization, four poly- and poly product generations are reduced, i.e., thus by control
Extent of polymerization can obtain the isoparaffin solvent oil of higher yield and higher purity.Therefore, in order to enter one
Step improves the purity of isoparaffin in the yield and solvent naphtha of isoparaffin solvent oil, under preferable case, step
Suddenly in (2), polymeric reaction condition includes：Temperature is 50~150 DEG C, preferably 100~130 DEG C；
Time is 30~120min, preferably 30~50min；Polymerization pressure is 0~0.5MPa of gauge pressure.Wherein,
Temperature can be 100 DEG C, 105 DEG C, 110 DEG C, 115 DEG C, 120 DEG C, 125 DEG C, 130 DEG C or foregoing number
Arbitrary value between value, time can be 30min, 35min, 40min, 45min, 50min or foregoing
Arbitrary value between numerical value, polymerization pressure can be gauge pressure 0MPa, 0.1MPa, 0.2MPa, 0.3MPa,
Arbitrary value between 0.4MPa, 0.5MPa or aforementioned value.
In the method for the present invention, for polymerization catalyst, there is no particular limitation, can be commonly used in the art
The various catalyst for olefinic polymerization, under preferable case, polymerization catalyst is Lewis acid catalysts,
It is further preferred that Lewis acid catalysts be aluminum halide, alkyl aluminium halide, alkyl aluminum, halogenation boron,
One kind or more in tin halides, iron halide, copper halide, halogenated titanium, antimony halides, zinc halide and gallium halide
Kind, the more preferably one or more in aluminum halide, alkyl aluminium halide, alkyl aluminum and halogenation boron,
Still more preferably it is the one or more in boron trifluoride, alchlor, aluminium ethide and Chloroethyl aluminium.
Halo groups in Lewis acid catalysts can be fluorine and/or chlorine, preferably chlorine.
Preferably, in the product that polymerization catalyst and step (1) obtain the mass ratio of alkene for (0.01~
0.1)：1, more preferably (0.02~0.06)：1.
Wherein, because Lewis acid catalysts are more sensitive to water, so depending on raw material condition, if any
It is necessary then need first raw material to be dried before reactions processing.Specific drying process condition is ability
Known to field technique personnel, it will not be repeated here.
In step (2), it is preferable that after polymerisation terminates, add alkali lye washing, standing separation
Polymerizate is post-processed again afterwards.
Heretofore described polymerisation can be in the polymerization reaction kettle of routine with gap or successive reaction
Mode carry out.
In the method for the present invention, the polymerizate for further obtaining the polymerisation be hydrogenated with instead
Should, it is saturated alkane that can not only convert the polymerizate, and can also realize will be in step (1)
The halogenated alkane progress hydrodehalogenation element formed is converted by alcohol and is converted into alkane.Under preferable case, step (3)
In, hydrogenation conditions include：Hydrogen dividing potential drop is 1~3MPa of gauge pressure；Temperature is 150~200 DEG C；Hydrogen
The volume ratio (i.e. hydrogen to oil volume ratio) for the product that gas obtains with step (2) is (100~400)：1；
Volume space velocity is 3~6h during the liquid for the product that step (2) obtains-1。
In the inventive method, the hydrogenation catalyst is loaded catalyst, containing active metal and carrier,
The active metal is selected from group vib and/or group VIIIB metal, under preferable case, in step (3),
The hydrogenation catalyst is the group vib metal and/or group VIIIB metallic catalyst being carried on carrier,
It is further preferred that carrier is in silica, aluminum oxide, clay, magnesia, titanium oxide and zirconium oxide
One or more；Group vib metal includes molybdenum and/or tungsten, and group VIII metal includes cobalt and/or nickel.
Preferably, in the hydrogenation catalyst, on the basis of the weight of hydrogenation catalyst, group vib metal
The content of oxide be 15~25 weight %, the oxide content of group VIIIB metal is 3~6 weight
%, the content of carrier is 72~80 weight %.
In the method for the present invention, the product of step (2) is contacted with hydrogen in the presence of a hydrogenation catalyst,
The saturation to alkene can be realized, the removal of impurity can also be realized, impurity is mainly the remaining in raw material
Micro amount of oxygen.
In the inventive method, step (4) can use conventional destilling tower to implement to step (3) product
Fractionation cutting, can use stepwise distillation, i.e. air-distillation is followed by evaporated under reduced pressure, wherein normal pressure steaming
Evaporate and cut to obtain 160 DEG C to 200 DEG C of cut；It is evaporated under reduced pressure, residual voltage is 10mmHg or so, is cut
200 DEG C to 340 DEG C of cut is obtained, collects obtain the isoparaffin solvent oil of the present invention together.
The cut obtained through the fractionation cutting is high-purity isoparaffin composition, can be according to different need
Seek the solvent naphtha for preparing different model.Also 160~340 DEG C of cut further can be cut as needed
Cut, to obtain the different cut of more boiling ranges, be used as the solvent naphtha of different purposes.
Second aspect, present invention also offers the isoparaffin solvent oil obtained by the above method, the isomery
Alkane solvent oil boiling range be 160 DEG C~340 DEG C, wherein, using the gross weight of the isoparaffin solvent oil as
Benchmark, the content of isoparaffin is more than 98 weight %；It is preferred that the oxygen of the isoparaffin solvent oil contains
It is below 0.05 volume % to measure as below 0.1 weight %, arene content.
In the present invention, the content of aromatic hydrocarbons uses arene content in the atoleines of SH/T 0409 to survey in solvent naphtha
Determine method (ultraviolet spectrophotometry) measure.
The present invention will be described in detail by way of examples below.
In following examples：
Lewis acid catalysts are the aluminum trichloride (anhydrous) (AlCl of Chinese medicines group3Content be >=99.0 weight
%)；
F- T synthesis light oil comes from coal liquifaction Chemical Co., Ltd. of Shenhua, and composition is shown in Table 1；
The solvent naphtha obtained in F- T synthesis light oil, F- T synthesis naphtha, embodiment and comparative example
Component and content are measured by chromatographic process；
The content of aromatic hydrocarbons uses arene content determination method in the atoleines of SH/T 0409 (ultraviolet in solvent naphtha
AAS) measure；
Solvent oil yield (being calculated by olefin(e) centent in F- T synthesis naphtha) is calculated by following formula：
Solvent oil yield %=[(quality of 160 DEG C~340 DEG C products in product)-(160 DEG C in raw material~
340 DEG C of alkane quality)] quality of alkene in/raw material } × 100%；
The yield of cut more than 340 DEG C is calculated by following formula：
More than 340 DEG C cut yield %=(are more than the matter of alkene in quality/raw material of 340 DEG C of products in product
Amount) × 100%；
Table 1
H-NMR signs are carried out to this F- T synthesis light oil raw material.The integral area at each peak is computed,
The 83.2 mass % that alpha-olefin in this F- T synthesis light oil accounts for total olefin can be calculated, interior alkene accounts for total alkene
16.8 mass % of hydrocarbon.The end point of distillation of this F- T synthesis light oil raw material is 360 DEG C.
Preparation example 1
F- T synthesis light oil is subjected to rectifying, cuts out cut of the end point of distillation no more than 160 DEG C as expense
Synthetic naphtha is held in the palm, is designated as FTN-1, composition is shown in Table 2 and table 3.
Table 2
Table 3
| Carbon number | N-alkanol | Isomery alcohol | Aldehyde | Ketone | Ester | It is total |
| 2 | 0.33 | 0 | 0 | 0 | 0 | 0.33 |
| 3 | 0.71 | 0 | 0 | 0 | 0 | 0.71 |
| 4 | 2.08 | 0.07 | 0.09 | 0.15 | 0 | 2.39 |
| 5 | 3.92 | 0.46 | 0.03 | 0 | 0.16 | 4.57 |
| 6 | 4.60 | 0.30 | 0 | 0.02 | 0.02 | 4.94 |
| 7 | 0.20 | 0.05 | 0 | 0 | 0 | 0.25 |
| It is total | 11.84 | 0.88 | 0.12 | 0.17 | 0.18 | 13.19 |
Preparation example 2
F- T synthesis light oil is subjected to rectifying, cuts out cut of the end point of distillation no more than 200 DEG C as expense
Synthetic naphtha is held in the palm, is designated as FTN-2, composition is shown in Table 4 and table 5.
Table 4
| Carbon number | N-alkane | Isoparaffin | Alkene | Cycloalkane | Aromatic hydrocarbons | It is total |
| 2 | 0 | 0 | 0 | 0 | 0 | 0 |
| 3 | 0 | 0 | 0 | 0 | 0 | 0 |
| 4 | 0.03 | 0 | 0.05 | 0 | 0 | 0.08 |
| 5 | 0.59 | 0.09 | 1.09 | 0 | 0 | 1.77 |
| 6 | 1.97 | 0.28 | 4.65 | 0.01 | 0 | 6.91 |
| 7 | 3.25 | 0.97 | 7.89 | 0.03 | 0.48 | 12.62 |
| 8 | 3.86 | 0.87 | 9.9 | 0.19 | 0.03 | 14.85 |
| 9 | 3.91 | 1.01 | 10.69 | 0.09 | 0.04 | 15.74 |
| 10 | 3.8 | 1.06 | 10.15 | 0 | 0.43 | 15.44 |
| 11 | 3.21 | 1 | 8 | 0 | 0.16 | 12.37 |
| 12 | 1.72 | 0.61 | 2.63 | 0 | 0 | 4.96 |
| It is total | 22.34 | 5.89 | 55.05 | 0.32 | 1.14 | 84.74 |
Table 5
| Carbon number | N-alkanol | Isomery alcohol | Aldehyde | Ketone | Ester | It is total |
| 2 | 0.2 | 0 | 0 | 0 | 0 | 0.2 |
| 3 | 0.43 | 0 | 0 | 0 | 0 | 0.43 |
| 4 | 1.26 | 0.04 | 0.11 | 0.09 | 0 | 1.5 |
| 5 | 2.38 | 0.28 | 0.02 | 0 | 0.1 | 2.78 |
| 6 | 3.4 | 0.36 | 0 | 0.01 | 0.01 | 3.78 |
| 7 | 2.71 | 0.18 | 0 | 0 | 0.01 | 2.9 |
| 8 | 2.19 | 0.12 | 0 | 0.05 | 0.03 | 2.39 |
| 9 | 1.22 | 0.06 | 0 | 0 | 0 | 1.28 |
| 10 | 0 | 0 | 0 | 0 | 0 | 0 |
| 11 | 0 | 0 | 0 | 0 | 0 | 0 |
| 12 | 0 | 0 | 0 | 0 | 0 | 0 |
| It is total | 13.79 | 1.04 | 0.13 | 0.15 | 0.15 | 15.26 |
Embodiment 1
This example demonstrates that the method for the F- T synthesis naphtha production isoparaffin solvent oil of the present invention.
(1) by F- T synthesis naphtha FTN-1, in catalyst, (concentrated hydrochloric acid containing anhydrous zinc chloride is molten
Liquid, wherein ZnCl2：HCl mol ratio is 1：1) effect is lower carries out alcohol chlorination, closes Fischer-Tropsch
Chloralkane is converted into the alcohol in naphtha, wherein, alcohol chlorination condition includes：Temperature is 50
DEG C, naphtha FTN-1 mixes with catalyst, and catalyst amount is F- T synthesis naphtha FTN-1's
50 volume %.Product after alcohol chlorination is subjected to static layering, takes upper strata product as polymerisation
Raw material.
(2) according to the polymerisation and hydrogenation conditions of table 6, the polymerization that step (1) is obtained is anti-
Raw material is answered to carry out polymerisation, obtained product is separated off catalyst, and the conduct after alkali cleaning and washing
Polymeric reaction product；
Hydrofinishing is carried out to polymerizate, the hydrogen consumption that hydrogenation reaction is calculated is 0.56%.To hydrogenation
Reaction product is distilled, and it is 160 DEG C~340 DEG C of cut as solvent oil product to obtain boiling range.
The solvent oil product is subjected to constituent analysis, wherein, isoparaffin content is 98.5 weight %, oxygen
Content is the weight % of ＜ 0.1 (detection line of instrument is 0.1%), and arene content is 0.03 volume %.Product
Appearance colorless is transparent.
The yield that solvent naphtha is calculated is 83.5%.The yield of cut more than 340 DEG C is 8.5%.
Embodiment 2
This example demonstrates that the method for the F- T synthesis naphtha production isoparaffin solvent oil of the present invention.
(1) by F- T synthesis naphtha FTN-1, in catalyst, (concentrated hydrochloric acid containing anhydrous zinc chloride is molten
Liquid, wherein ZnCl2：HCl mol ratio is 1：1) effect is lower carries out alcohol chlorination, closes Fischer-Tropsch
Chloralkane is converted into the alcohol in naphtha, wherein, alcohol chlorination condition includes：Temperature is 60
DEG C, naphtha FTN-1 mixes with catalyst, and catalyst amount is F- T synthesis naphtha FTN-1's
50 volume %.Product after alcohol chlorination is subjected to static layering, takes upper strata product as polymerisation
Raw material.
(2) according to the polymerisation and hydrogenation conditions of table 6, the polymerization that step (1) is obtained is anti-
Answer raw material to carry out polymerisation, hydrofinishing is carried out to polymerizate, the hydrogen consumption of hydrogenation reaction is calculated
For 0.58%.Hydrogenation reaction product is distilled, obtains the cut solvent that boiling range is 160 DEG C~340 DEG C
Oil product.
The solvent oil product is subjected to constituent analysis, wherein, isoparaffin content is 99.1 weight %, oxygen
Content is the weight % of ＜ 0.1, and arene content is 0.04 volume %.Product appearance water white transparency.
The yield that solvent naphtha is calculated is 89.2%.The yield of cut more than 340 DEG C is 4.8%.
Embodiment 3
This example demonstrates that the method for the F- T synthesis naphtha production isoparaffin solvent oil of the present invention.
(1) by F- T synthesis naphtha FTN-1, in catalyst, (concentrated hydrochloric acid containing anhydrous zinc chloride is molten
Liquid, wherein ZnCl2：HCl mol ratio is 1：1) effect is lower carries out alcohol chlorination, closes Fischer-Tropsch
Chloralkane is converted into the alcohol in naphtha, wherein, alcohol chlorination condition includes：Temperature is 30
DEG C, naphtha FTN-1 mixes with catalyst, and catalyst amount is F- T synthesis naphtha FTN-1's
50 volume %.Product after alcohol chlorination is subjected to static layering, takes upper strata product as polymerisation
Raw material.
(2) according to the polymerisation and hydrogenation conditions of table 6, the polymerization that step (1) is obtained is anti-
Raw material is answered to carry out polymerisation, obtained product is separated off catalyst, and the conduct after alkali cleaning and washing
Polymeric reaction product；
Polymeric reaction product is distilled, it is smart as hydrogenation to obtain the cut that boiling range is 160 DEG C~340 DEG C
The raw material of system simultaneously carries out hydrofinishing, obtained solvent oil product.Be calculated hydrogenation reaction hydrogen consumption be
0.40%.
The solvent oil product is subjected to constituent analysis, wherein, isoparaffin content is 99.0 weight %, oxygen
Content is the weight % of ＜ 0.1, and arene content is 0.03 volume %.Product appearance water white transparency.
The yield that solvent naphtha is calculated is 84.2%.The yield of cut more than 340 DEG C is 6.0%.
Table 6
* Ni is using the content that NiO is counted as 4 weight %, and Mo is with MoO3The content of meter is 24 weight %；
Remaining is Al2O3。
Embodiment 4
According to the method for embodiment 1, the difference is that, with " 80 DEG C of polymerization temperature " replacement " polymerization temperature
100 DEG C ", produced to obtain solvent naphtha.
The hydrogen consumption of hydrogenation reaction is 0.58%.
The solvent oil product of acquisition is subjected to constituent analysis, wherein, isoparaffin content is 98.2 weight %,
Oxygen content is<0.1 weight %, arene content are 0.04 volume %.Product appearance water white transparency.
The yield that solvent naphtha is calculated is 77.6%.The yield of cut more than 340 DEG C is 4.2%.
Embodiment 5
According to the method for embodiment 1, the difference is that, so that " polymerization time replaces " polymerization as 80min "
Time is 50min ", is produced to obtain solvent naphtha.
The hydrogen consumption of hydrogenation reaction is 0.58%.
The solvent oil product of acquisition is subjected to constituent analysis, wherein, isoparaffin content is 98.3 weight %,
Oxygen content is<0.1 weight %, arene content are 0.03 volume %.Product appearance water white transparency.
The yield that solvent naphtha is calculated is 75.3%.The yield of cut more than 340 DEG C is 4.2%.
Embodiment 6
According to the method for embodiment 1, the difference is that, with " FTN-2 " replacement " FTN-1 ", given birth to
Production obtains solvent naphtha.
The hydrogen consumption of hydrogenation reaction is 0.54%.
The solvent oil product of acquisition is subjected to constituent analysis, wherein, isoparaffin content is 70.2 weight %,
Oxygen content is 0.65 weight %, and arene content is 1.2 volume %.
The yield that solvent naphtha is calculated is 61.3%.The yield of cut more than 340 DEG C is 30.5%.
Embodiment 1 is understood compared with embodiment 4-5, the temperature of polymerisation is 100~130 DEG C, when
Between when being 30~50min, can further improve the obtained yield of isoparaffin solvent oil.
Embodiment 1 is understood compared with embodiment 4-5, the temperature of polymerisation is 100-130 DEG C, when
Between when being 30-50min, can further improve the obtained yield of isoparaffin solvent oil.
Embodiment 1 is understood compared with embodiment 6,160 DEG C of F- T synthesis is not more than using the end point of distillation
When naphtha is as raw material, the obtained purity of isoparaffin solvent oil can be further improved.
Comparative example 1
According to the method for embodiment 1, the difference is that, with the F- T synthesis lightweight in CN104560193A
Oily A substitutes " FTN-1 ", is produced to obtain solvent naphtha.
The hydrogen consumption of hydrogenation reaction is 0.47%.
The solvent oil product of acquisition is subjected to constituent analysis, wherein, isoparaffin content is 51.2 weight %,
Oxygen content is 0.15 weight %, and arene content is 0.04 volume %.
The yield that solvent naphtha is calculated is 35.2%.The yield of cut more than 340 DEG C is 60.3%.
The present invention is can be seen that from the result of embodiment and comparative example 1 and obtains isoparaffin solvent oil, is received
Rate is high, and isoparaffin content is high.
The F- T synthesis light oil A in CN104560193A is used to carry out production solvent in comparative example 1
Oil.In CN104560193A, solvent naphtha is produced using F- T synthesis light oil A, need to be in hydrogen point
Press 10MPa, volume space velocity 1.2h-1, be hydrogenated with 330 DEG C of hydrogen to oil volume ratio 600 and reaction temperature
Isomerization reaction, higher than the temperature and hydrogen dividing potential drop of the Hydrofinishing conditions of embodiment 1, processing severity is more
It is high.The volume space velocity of additional embodiment 1 is higher, illustrates that the ability of unit time-triggered protocol is bigger.Compared to existing
There is technology, method of the invention can use the hydroconversion condition more relaxed, have higher disposal ability,
With more preferable industrial applications prospect.
Comparative example 2
According to the polymerisation of embodiment 1 in table 6 and the reaction condition of hydrofinishing, by F- T synthesis stone
Cerebrol FTN-1 carries out polymerisation, and obtained product is separated off catalyst, and after alkali cleaning and washing
As polymeric reaction product；
Polymeric reaction product is distilled, it is smart as hydrogenation to obtain the cut that boiling range is 160 DEG C~340 DEG C
The raw material of system simultaneously carries out hydrofinishing, obtained solvent oil product.Be calculated hydrogenation reaction hydrogen consumption be
0.58%.
The solvent oil product is subjected to constituent analysis, wherein, isoparaffin content is 95.4 weight %, oxygen
Content is 0.2 weight %, and arene content is 0.04 volume %.
The yield that solvent naphtha is calculated is 52.3%.The yield of cut more than 340 DEG C is 6.5%.
It can be seen that from the result of embodiment 1 and comparative example 2 and reduce alcohol halogenating reaction step, alcohol is to poly-
Closing reaction has negative effect, causes the inactivation of polymerization catalyst, makes solvent in the case of same catalyst amount
The yield step-down of oil.
The preferred embodiment of the present invention described in detail above, still, the present invention are not limited to above-mentioned reality
The detail in mode is applied, can be to the technical side of the present invention in the range of the technology design of the present invention
Case carries out a variety of simple variants, and these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique described in above-mentioned embodiment is special
Sign, in the case of reconcilable, can be combined by any suitable means, in order to avoid need not
The repetition wanted, the present invention no longer separately illustrate to various combinations of possible ways.
In addition, various embodiments of the present invention can be combined randomly, as long as its
Without prejudice to the thought of the present invention, it should equally be considered as content disclosed in this invention.
Claims (10)
1. a kind of method of F- T synthesis naphtha production isoparaffin solvent oil, including：
(1) F- T synthesis naphtha is subjected to alcohol halogenating reaction under catalyst action, makes F- T synthesis
Alcohol in naphtha is converted into halogenated alkane；
(2) product that step (1) obtains is subjected to polymerisation in the presence of polymerization catalyst, makes step
Suddenly the alkene in the product that (1) obtains is converted into target product as the poly- of dimerization compound and/or trimerization compound
Close product；
(3) product that step (2) obtains is subjected to hydrogenation reaction in the presence of a hydrogenation catalyst, makes step
Suddenly the polymerizate in the product that (2) obtain is converted into saturated alkane, while the production that step (2) obtains
Halogenated alkane dehalogenate in thing is converted into alkane；
(4) by be fractionated in the product of cutting step (3) initial boiling point not less than 160 DEG C and the end point of distillation not
Cut more than 340 DEG C, obtains isoparaffin solvent oil.
2. according to the method for claim 1, wherein, the F- T synthesis naphtha is the end point of distillation
F- T synthesis naphtha no more than 160 DEG C, wherein, using the gross weight of the F- T synthesis naphtha as
Benchmark, the F- T synthesis naphtha contain alkene more than 20 weight %；With the gross weight of the alkene
On the basis of amount, the content of alpha-olefin is less than 85 weight % in the alkene.
3. method according to claim 1 or 2, wherein, the F- T synthesis naphtha contains
Alkene, organic oxygen-containing compound and alkane, it is described on the basis of the F- T synthesis naphtha gross weight
Olefin(e) centent is 30~80 weight %；The organic oxygen-containing compound content is 1~30 weight %；It is described
Determination of Alkane Content is 20~40 weight %；
Preferably, on the basis of the F- T synthesis naphtha gross weight, in the organic oxygen-containing compound
Alcohol content is 1~25 weight %, preferably 10~20 weight %；
Preferably, on the basis of the gross weight of the alkene, in the alkene content of alpha-olefin be 10~
84.5 weight %.
4. according to the method described in any one in claim 1-3, wherein, in step (1), institute
Stating alcohol halogenating reaction condition includes：Temperature is 25~80 DEG C, preferably 30~60 DEG C.
5. according to the method described in any one in claim 1-4, wherein, in step (1), take
The catalyst for holding in the palm synthetic naphtha progress alcohol halogenating reaction is anhydrous zinc chloride or sulfuric acid；It is preferred that Fischer-Tropsch closes
The catalyst that alcohol halogenating reaction is carried out into naphtha is the concentrated hydrochloric acid solution containing anhydrous zinc chloride.
6. according to the method described in any one in claim 1-5, wherein, in step (2), institute
Stating polymeric reaction condition includes：Temperature is 50~150 DEG C, preferably 100~130 DEG C；Time be 30~
120min, preferably 30~50min；Polymerization pressure is 0~0.5MPa of gauge pressure.
7. according to the method described in any one in claim 1-6, wherein, in step (2), institute
It is Lewis acid catalysts to state polymerization catalyst, it is preferable that the Lewis acid catalysts be aluminum halide,
Alkyl aluminium halide, alkyl aluminum, halogenation boron, tin halides, iron halide, copper halide, halogenated titanium, antimony halides,
One or more in zinc halide and gallium halide, more preferably aluminum halide, alkyl aluminium halide, alkyl
One or more in aluminium and halogenation boron, it is still more preferably boron trifluoride, alchlor, aluminium ethide
With the one or more in Chloroethyl aluminium；
Preferably, the mass ratio of alkene is in the product that the polymerization catalyst obtains with step (1)
(0.01~0.1)：1, more preferably (0.02~0.06)：1.
8. according to the method described in any one in claim 1-7, wherein, in step (3), institute
Stating hydrogenation conditions includes：Hydrogen dividing potential drop is 1~3MPa of gauge pressure；Temperature is 150~200 DEG C；Hydrogen
The volume ratio of the product obtained with step (2) is (100~400)：1；The product that step (2) obtains
Liquid when volume space velocity be 3~6h-1。
9. according to the method described in any one in claim 1-8, wherein, in step (3), institute
It is the group vib metal and/or group VIIIB metallic catalyst being carried on carrier to state hydrogenation catalyst,
Preferably, the carrier is silica, aluminum oxide, clay, magnesia, titanium oxide and zirconium oxide
In one or more；
Preferably, the group vib metal includes molybdenum and/or tungsten, the group VIII metal include cobalt and/
Or nickel.
10. the isoparaffin solvent oil that the method according to any one in claim 1-9 obtains,
The boiling range of the isoparaffin solvent oil is 160 DEG C~340 DEG C, it is characterised in that with the Isopars
On the basis of the gross weight of oil, the content of isoparaffin is more than 98 weight %；It is preferred that the isoparaffin
The oxygen content of solvent naphtha is below 0.1 weight %, and arene content is below 0.05 volume %.
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Address after: 100011 Beijing Dongcheng District, West Binhe Road, No. 22 Patentee after: CHINA ENERGY INVESTMENT Corp.,Ltd. Patentee after: Beijing low carbon clean energy research institute Address before: 100011 Shenhua building, 22 West Binhe Road, Dongcheng District, Beijing Patentee before: SHENHUA GROUP Corp.,Ltd. Patentee before: Beijing low carbon clean energy research institute |