CN106699501A - Method for producing elemental N-alkanes - Google Patents
Method for producing elemental N-alkanes Download PDFInfo
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- CN106699501A CN106699501A CN201510781150.5A CN201510781150A CN106699501A CN 106699501 A CN106699501 A CN 106699501A CN 201510781150 A CN201510781150 A CN 201510781150A CN 106699501 A CN106699501 A CN 106699501A
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- alkane
- simple substance
- tower
- rectifying column
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- 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
- C10G7/00—Distillation of hydrocarbon oils
-
- 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
- C10G2300/1022—Fischer-Tropsch products
Abstract
The invention relates to the field of chemical engineering, and discloses a method for producing elemental N-alkanes. The method comprises the following steps of a pretreatment step, namely sequentially putting raw materials into a main fractionation tower and a stabilizer, and carrying out distillation under the effects of certain pressure and temperature to obtain stable distillate; and a distillation step, namely putting the stable distillate into fractionation towers, carrying out fractionation under the effects of certain pressure and temperature to obtain elemental N-alkanes, wherein the number of the fractionation towers is 2N-1; the variety number of the obtained elemental N-alkanes is N; and N is an integer of 1-6. The production technology of the elemental N-alkanes is simple and feasible, a product is convenient and fast to separate, the equipment investment is reduced and the energy consumption is reduced.
Description
Technical field
The present invention relates to chemical field, more particularly to a kind of method for producing simple substance n-alkane.
Background technology
The production main method of existing C5~C10 simple substance n-alkane is：With naphtha as raw material, through dividing
N-alkane and non-n-alkane in son sieve adsorbing separation naphtha, are adsorbent using 5A molecular sieves,
With rudimentary n-alkane, ammonia, hydrogen or water vapour etc. as desorbing agent, using the selection of 5A molecular sieves
Absorption property, industrially realizes separating the n-alkane in naphtha, to obtain high-purity
N-alkane, then obtain simple substance n-alkane through rectifying.
In this generating process, existing technique for extracting high-pure normal hexane product by pressure swing adsorption, using four
Tower heats pressure-variable adsorption flow, and the desorption of adsorbent n-hexane is realized under vacuum, through rectifying column point
N-hexane of the purity more than 99% is obtained after.There is pressure-variable adsorption to extract normal heptane coproduction normal octane now
Technique, pressure-variable adsorption flow is heated using multitower, adds inert gas to be blown while vacuum desorption
Sweep, bed is sufficiently desorbed, coproduction obtains the normal heptane and normal octane that purity is all higher than 99%.
The existing method that the separating normal alkane from C5~C6 alkane isomerization products has been proposed, it is real
Show the separation under liquid-phase condition, using the isopentane in rectification method removing raw material, reuse absorption method suction
Fufen, using normal octane as liquid phase strippant, is parsed from positive isoparaffin mixed material to bed.
It is existing to also disclose C4~C6 n-alkane coproduction isopentane and isomery hexane in a kind of extraction light naphthar
Technique, using multi-tower variable pressure adsorption and rectifying separation coupling technique.
Prior art is usually that, with petroleum product as raw material, petroleum composition is complicated, containing aromatic hydrocarbons, cycloalkane,
S, N, O etc., and molecular sieve in itself the characteristics of, production simple substance n-alkane requirement raw material not sulfur-bearing,
Complicated to the preprocessing process with oil as raw material, long flow path, investment is big.In addition, in production process often
Desorbing agent is micro-molecular gas, it is desirable to which subsequent condensation temperature is low, even up to subzero, it is desirable to condense
Pressure is higher, and energy consumption and equipment investment are larger, there is desorbing agent consumption height, desorption and regeneration in real process
Difficult the problems such as.Furthermore, the composition of petroleum distillate raw material is complicated, and the overlapping boiling points of different component are more,
Positive structure, anon-normal structure component boiling point it is close (such as 68.7 DEG C of n-hexane boiling point, 71.8 DEG C of methyl cyclopentane boiling point,
Both only 3.1 DEG C of differences), and isomeric component content is higher, energy consumption big using rectification method separating difficulty
It is high, it is impossible to which that serial simple substance n-alkane is produced by simpler method.Must first to n-alkane and its
Its non-normal hydrocarbons is first separated, and then obtains the purity positive structure of simple substance higher using the method for rectifying again
Alkane, complex technical process.Simultaneously when first step n-alkane is separated with other non-normal hydrocarbons, inhaling
, it is necessary to expend substantial amounts of energy in attached desorption process, the economy of whole device is reduced.
The content of the invention
It is an object of the invention to provide the side that a kind of utilization Fischer-Tropsch synthetic produces simple substance n-alkane
Method, simple production process is easy, and it is convenient that product is separated, and reduces equipment investment, reducing energy consumption.
In order to solve the above technical problems, embodiments of the present invention provide a kind of production simple substance n-alkane
Method, comprise the steps of：
Pre-treatment step：It is sequentially placed into Fischer-Tropsch synthetic as raw material in main fractionating tower and stabilizer,
The rectifying under certain pressure and temperature action, obtains stabilization distillate oil；
Rectification step：The stabilization distillate oil is put into rectifying column, under certain pressure and temperature action
Rectifying, obtains simple substance n-alkane；
Wherein, the species number of the required simple substance n-alkane for obtaining is N kinds, and the quantity of the rectifying column is
2N-1；The N is any one integer in 1 to 6.
In terms of existing technologies, the main distinction and its effect are embodiment of the present invention：Using containing
The Fischer-Tropsch synthetic production simple substance n-alkane of n-alkane higher proportion, separates simple, raising product
Added value, make the maximizing the benefits of F- T synthesis technology.
If as a further improvement, the quantity of the rectifying column is more than 1, further limiting needs multiple
Rectifying column, product separation sequence is included with one of Types Below, or its any combination：I.e. the first kind according to
The boiling point of product simple substance n-alkane isolates isohydrocarbon and positive structure under each carbon number successively from low to high
Hydrocarbon, or isolate the isohydrocarbon under each carbon number successively from high to low according to product simple substance n-alkane boiling point
And normal hydrocarbon.Second Type can be first cut into weight component between any two kinds of n-alkanes, then
The boiling point order for simple substance n-alkane contained by weight component separates the isomery under each carbon number successively respectively
Hydrocarbon and normal hydrocarbon.3rd type is first to isolate to be first cut into being the isohydrocarbon under certain carbon number according to carbon number
With the mixture of normal hydrocarbon, then by the isolated isohydrocarbon of the mixture and normal hydrocarbon.On 4th type is
State the combination of three types.Above-mentioned various separation sequences are finally attained by isolating simple substance n-alkane product
The purpose of product.
Any separation sequence is used in actual applications, should be contained according to each component in Fischer-Tropsch synthetic
Situations such as amount, treating capacity, makees specific analysis, specifically, preferentially using conventional distillation, measures big component
Preferentially separate, the best equimolar of product of tower top and tower reactor is separated.
As a further improvement, the operating condition of each rectifying column is respectively：Rectifying column both can be plate
Formula tower can also be packed tower, 20~120 pieces of number of theoretical plate, Rectification column pressure opereating specification
0.05MPa~1.0MPa, 40~200 DEG C of tower top operation temperature, 60~200 DEG C of tower reactor operation temperature.
When further restriction needs to obtain various simple substance n-alkanes, component analysis is carried out to raw material, selected
Specific separation sequence, is calculated by simulating, it is determined that the operating condition of each rectifying column for needing, it is ensured that
The acquisition of each simple substance n-alkane.
Brief description of the drawings
Fig. 1 is the method flow diagram of the production simple substance n-alkane in first embodiment of the invention；
Fig. 2 is the method flow diagram of the production simple substance n-alkane in second embodiment of the invention；
Fig. 3 is the method flow diagram of the production simple substance n-alkane in third embodiment of the invention.
Specific embodiment
To make the object, technical solutions and advantages of the present invention clearer, below in conjunction with accompanying drawing to this hair
Bright each implementation method is explained in detail.However, it will be understood by those skilled in the art that
In each implementation method of the invention, in order that reader more fully understands the application and to propose many technologies thin
Section.But, even if many variations and modification without these ins and outs and based on following implementation method,
The application each claim technical scheme required for protection can also be realized.
First embodiment of the invention is related to a kind of method for producing simple substance n-alkane.Present embodiment
According to the boiling point of product simple substance n-alkane isolate successively from low to high isohydrocarbon under each carbon number and
Normal hydrocarbon.Concrete technology flow process figure is as shown in figure 1, specific as follows：
Pre-treatment step：Main fractionating tower 101 and stabilizer 102 are put into using Fischer-Tropsch synthetic as raw material
In, the rectifying under certain pressure and temperature action obtains stabilization distillate oil.
Specifically, in pre-treatment step, using the boiling-point difference of component, unwanted heavy constituent is pulled out
And light component.Fischer-Tropsch synthetic first passes through heating, subsequently into main fractionating tower 101, in main fractionating tower
In 101, normal boiling point (NBP) is cut higher than the heavy constituent that n-alkane boiling point is obtained required for certain
Out, while on-condensible gas composition is sent to fuel system as gas phase from tower top, tower top liquid phase is used as separation
The raw material of simple substance normal hydrocarbon is sent to stabilizer 102.In present embodiment, removed from Fischer-Tropsch synthetic
LPG (Liquefied Petroleum Gas, liquefied petroleum gas) and most C11 containing C5 isomeries
Above component.
It should be noted that main fractionating tower 101 can attach side line tower, specifically, side line tower band 1,
2 or 3 side lines, for cutting out different liquid wax products simultaneously.For certain side line tower, liquid
Body is extracted out from certain layer of column plate of king-tower, and side line tower is entered after extraction, and tower reactor is heated or stripped using reboiler
Agent is stripped, and preferentially from steam stripping, material is from certain block theoretical plate liquid phase, the gas of side line tower in king-tower
Phase discharging opening returns to the upper strata theoretical plate of the discharging opening of king-tower, side line tower tower reactor Produced Liquid wax product.Value
Obtain one and be mentioned that side line tower both can be plate column, or packed tower.
In particular, the return tank of top of the tower of main fractionating tower 101 is solution-air-liquid knockout drum, and water does not flow back mutually
To in king-tower, oil phase is flowed back, and thick distillate oil is produced by reflux pump；King-tower tower reactor uses steam stripping agent
Stripping, steam stripping agent can use steam, nitrogen or carbon dioxide, preferentially from steam stripping, main fractionating tower 101
Tower reactor produces heavy liquid wax.Furtherly, the operating condition of main fractionating tower 101 can be as follows：Operation pressure
0.1~0.3MPa of power, tower top temperature is 100~200 DEG C (preferably 110~140 DEG C), bottom temperature
200~300 DEG C, 5~50 pieces of main fractionating tower number of theoretical plate, 2~10 pieces of side line tower number of theoretical plate.
The oil phase of the tower top of main fractionating tower 101 is delivered to stabilizer 102 and is further separated.Mentioned above
Stabilizer 102, the backflow of tower top band, less than the hydrocarbon component of pentane, tower reactor is with again for overhead extraction boiling point
Boiling device heating, tower reactor extraction is equal to the cut higher than pentane comprising boiling point.Specifically, stabilizer 102
Operating condition can be as follows：1.0~2.0MPa of operating pressure, prioritizing selection 1.5MPa, tower top temperature
It is 80~160 DEG C (preferably 110~140 DEG C), 200~250 DEG C of bottom temperature.Through stabilizer 102
Stabilization distillate oil is obtained afterwards.It is noted that stabilizer both can be plate column, or filler
Tower.
Above-mentioned is exactly the concrete operations of pre-treatment step, then carries out step：The stabilization distillate oil is put
In entering rectifying column (both can be that plate column can also be packed tower), under certain pressure and temperature action
Rectifying, obtains simple substance n-alkane.
Specifically, carried out specifically as a example by needing to obtain six kinds of simple substance n-alkanes in present embodiment
Bright, six kinds of simple substance n-alkanes are respectively：Pentane, n-hexane, normal heptane, normal octane, n -nonane,
N-decane.
In rectification step, the species of the quantity of the rectifying column for being used and the simple substance n-alkane for being obtained
Number has certain relation, and specifically, the species number of the required simple substance n-alkane for obtaining is N kinds, institute
The quantity of the rectifying column of setting is 2N-1；Wherein, N is any one integer in 1 to 6.Through each set
Rectifying column, simple substance n-alkane, all kinds of isoparaffins and heavy constituent needed for isolating successively, wherein,
Heavy constituent will return to pretreatment unit.
6 kinds of simple substance n-alkanes are isolated needed for present embodiment, so the rectifying column quantity that need to be used
It is 11.Technological process to each rectifying column below is specifically described：
The stable distillate oil (stablizing naphtha) that rectifying column 103 will be obtained from stabilizer 102, point
Separate out pentane, and C6~C10, heavy component mixture.The operating pressure of rectifying column 103 according to
Depending on the cooling water condition of overhead condenser, this example is 0.15~0.25MPa, and tower top temperature is with operating pressure
And tower top composition change and change, this example be 47~67 DEG C.By C6~C10 therein, heavy group
The mixture for dividing is sent to rectifying column 104.
Rectifying column 104 therefrom isolates C6 isomeries, and n-hexane, C7~C10, heavy component is mixed
Compound, 0.05~0.15MPa of its operating pressure, the change that tower top temperature is constituted with operating pressure and tower top
And change, this example is 51~71 DEG C.By n-hexane therein, C7~C10, heavy component mixture
It is sent to rectifying column 105.
Rectifying column 105 therefrom isolates n-hexane, with C7~C10, the mixture of heavy component, rectifying
0.05~the 0.15MPa of operating pressure of tower 105, the change that tower top temperature is constituted with operating pressure and tower top
And change, this example is 59~79 DEG C.The mixture of C7~C10 therein, heavy component is sent to rectifying
Tower 106.
Rectifying column 106 therefrom isolates C7 isomeries, with normal heptane, C8~C10, heavy component it is mixed
Compound.0.05~the 0.15MPa of operating pressure of rectifying column 106, tower top temperature is with operating pressure and tower top
The change of composition and change, this example be 80~100 DEG C.By normal heptane therein, C8~C10, heavy group
The mixture for dividing is sent to rectifying column 107.
Rectifying column 107 therefrom isolates normal heptane, with C8~C10, the mixture of heavy component.Rectifying
0.05~the 0.15MPa of operating pressure of tower 107, the change that tower top temperature is constituted with operating pressure and tower top
And change, this example is 90~110.The mixture of C8~C10 therein, heavy component is sent to rectifying column
108。
Rectifying column 108 therefrom isolates C8 isomeries, with normal octane, C9~C10, heavy component it is mixed
Compound.0.05~the 0.15MPa of operating pressure of rectifying column 108, tower top temperature is with operating pressure and tower top
The change of composition and change, this example be 108~130.By normal octane therein, C9~C10, heavy group
The mixture for dividing is sent to rectifying column 109.
Rectifying column 109 therefrom isolates normal octane, with C9~C10, the mixture of heavy component.Rectifying
0.05~the 0.15MPa of operating pressure of tower 109, the change that tower top temperature is constituted with operating pressure and tower top
And change, this example is 116~136.The mixture of C9~C10 therein, heavy component is sent to rectifying
Tower 110.
Rectifying column 110 therefrom isolates C9 isomeries, is just appointing the mixture of alkane, C10, heavy component.Essence
Evaporate the 0.05~0.15MPa of operating pressure of tower 110, the change that tower top temperature is constituted with operating pressure and tower top
Change and change, this example is 135~155.The mixture for just appointing alkane, C10, heavy component therein is sent to
Rectifying column 111.
Isolated in rectifying column 111 and just appoint alkane, with C10, the mixture of heavy component.Rectifying column 111
0.05~0.15MPa of operating pressure, tower top temperature becomes with the change that operating pressure and tower top are constituted
Change, this example is 141~161.The mixture of C10 therein, heavy component is sent to rectifying column 112.
Rectifying column 112 therefrom isolates C10 isomeries, with positive flow silane, the mixture of heavy component.Rectifying
0.05~the 0.15MPa of operating pressure of tower 112, the change that tower top temperature is constituted with operating pressure and tower top
And change, this example is 156~176.The mixture of positive flow silane therein, heavy component is sent to rectifying column
113。
Rectifying column 113 therefrom isolates positive flow silane and heavy component, and heavy component returns to main fractionating tower 101.
0.05~the 0.15MPa of operating pressure of rectifying column 113, tower top temperature is constituted with operating pressure and tower top
Change and change, this example is 162~184.
It is noted that during above-mentioned rectifying column 103 to rectifying column 113 can also regard rectification cell as
The first tower, the second tower, the 3rd tower ..., the 11st tower.After this 11 treatment of tower, six
Plant simple substance n-alkane (pentane, n-hexane, normal heptane, normal octane, n -nonane, n-decane) quilt
Separate successively.Above-mentioned rectifying column 103 to the operating pressure and operation temperature of rectifying column 113 is pushing away for this example
Recommend value, not limited to this value.
Embodiment of the present invention in terms of existing technologies, due to Fischer-Tropsch synthetic without sulphur without aromatic hydrocarbons,
Without heterocyclic compound, the isomers species of contained isohydrocarbon is few, the essentially α and β isomery of monomethyl
There is obvious gap in body, its boiling point, and content is also relatively fewer with normal hydrocarbon boiling point, therefore by direct
The method production of rectifying can simplify the technological process of simple substance n-alkane.It can be seen that, with Fischer-Tropsch synthetic
It is raw material, with the method for simple rectifying, substep obtains the simple substance n-alkane product with high added value,
Open the new technology road of a non-petroleum feedstocks using Fischer-Tropsch synthetic production simple substance n-alkane
Line, expand simple substance n-alkane carrys out source range.Its product quality is improve so that production Fischer-Tropsch is closed
Simple for process into the maximization of economic benefit of product, equipment investment is small, and overall energy consumption is low.
It is noted that present embodiment is in actual applications, can according to the boiling point of component height from
It is low to high or separate successively from high to low, it is also possible to be first first cut into as different under each carbon number according to carbon number
The mixture of structure hydrocarbon and normal hydrocarbon, then by the isolated isohydrocarbon of the mixture and normal hydrocarbon.
Second embodiment of the present invention is related to a kind of method for producing simple substance n-alkane.Second embodiment party
Formula is roughly the same with first embodiment, and main distinction part is：In the first embodiment, rectifying
Each rectifying column in unit is sequentially connected.And in second embodiment of the invention, first first cut according to carbon number
It is the isohydrocarbon and the mixture of normal hydrocarbon under each carbon number to be cut into, then by the isolated isomery of the mixture
Hydrocarbon and normal hydrocarbon.It can be seen that, the present invention can select different rectifying column connected modes with flexible and changeable, fit
For the different demands of different user.
The preprocessed unit of Fischer-Tropsch synthetic, removal containing C5 isomeries LPG and most C11 with
Upper component, through the rectifying column 4 in rectification cell, rectifying column 6, rectifying column 8, rectifying column 10 and rectifying
Tower 12, isolates pentane, C6 components, C7 components, C8 components, C9 components and C10 groups successively
Point.
Recycle rectifying column 5 that C6 isomeries and n-hexane are separated from C6 components；Rectifying column 7 is from 7 groups of C
C7 isomeries and normal heptane are separated in point；Rectifying column 9 separates C8 isomeries and normal octane from C8 components；
Rectifying column 11 separates C9 isomeries and n -nonane from C9 components；Rectifying column 13 is separated from C10 components
C10 isomeries and n-decane.Finally, the heavy constituent in rectifying column 12 returns to pretreatment unit.Pretreatment is single
Unit includes main fractionating tower and stabilizer.
Process chart in present embodiment is as shown in Fig. 2 specific as follows：
Fischer-Tropsch synthetic is added into main fractionating tower 201, naphtha, liquid paraffin,light and weight is separated into
Matter atoleine.The operating condition of main fractionating tower 201 is identical with first embodiment.
The distillate oil of main fractionating tower 201 delivers to distillate oil stabilizer 202, isolates LPG components and C5
Stable distillate oil above.The operating condition of stabilizer 202 is identical with first embodiment；
The stable naphtha that stabilizer 202 is obtained is sent to rectifying column 203, isolates pentane and more than C6
The mixture of component.Depending on the operating pressure of rectifying column 203 is according to the cooling water condition of overhead condenser,
This example is 0.15~0.25MPa；Tower top temperature changes with the change that operating pressure and tower top are constituted, this
Example is 47~67 DEG C.
The mixture of more than the C6 components that rectifying column 203 is obtained is sent to rectifying column 204, isolates C6 groups
Divide the mixture with more than C7 components；0.05~the 0.15MPa of operating pressure of rectifying column 204；Tower top temperature
Spend and change with the change that operating pressure and tower top are constituted, this example is 58~78 DEG C.
The C6 components that rectifying column 204 is obtained are sent to rectifying column 205, isolate C6 isomeries and n-hexane；
0.05~the 0.15MPa of operating pressure of rectifying column 205；Tower top temperature is constituted with operating pressure and tower top
Change and change, this example is 50~70 DEG C.
The mixture of more than the C7 components that rectifying column 204 is obtained is sent to rectifying column 206, isolates C7 groups
Divide the mixture with more than C8 components；0.05~the 0.15MPa of operating pressure of rectifying column 206；Tower top temperature
Spend and change with the change that operating pressure and tower top are constituted, this example is 85~105 DEG C.
The C7 components that rectifying column 206 is obtained are sent to rectifying column 207, isolate C7 isomeries and normal heptane；
0.05~the 0.15MPa of operating pressure of rectifying column 207, tower top temperature is constituted with operating pressure and tower top
Change and change, this example is 67~87 DEG C.
The mixture of more than the C8 components that rectifying column 206 is obtained is sent to rectifying column 208, isolates C8 groups
Divide the mixture with more than C9 components.0.05~the 0.15MPa of operating pressure of rectifying column 208；Tower top temperature
Spend and change with the change that operating pressure and tower top are constituted, this example is 108~128 DEG C.
The C8 components that rectifying column 208 is obtained are sent to rectifying column 209, isolate C8 isomeries and normal octane；
0.05~the 0.15MPa of operating pressure of rectifying column 209, tower top temperature is constituted with operating pressure and tower top
Change and change, this example is 88~108 DEG C.
The mixture of more than the C9 components that rectifying column 208 is obtained is sent to rectifying column 210, isolates C9 groups
Divide with C10 with the mixture of component；0.05~the 0.15MPa of operating pressure of rectifying column 210；Tower top temperature
Change with the change that operating pressure and tower top are constituted, this example is 130~150 DEG C.
The C9 components that rectifying column 210 is obtained are sent to rectifying column 211, isolate C9 isomeries and just appoint alkane；
0.05~the 0.15MPa of operating pressure of rectifying column 211；Tower top temperature is constituted with operating pressure and tower top
Change and change, this example is 115~136 DEG C.
The mixture of more than the C10 components that rectifying column 210 is obtained is sent to rectifying column 212, isolates separation
Go out C10 components and heavy component；Heavy component returns to main fractionating tower 201；The operation pressure of rectifying column 212
0.05~0.15MPa of power；Tower top temperature changes with the change that operating pressure and tower top are constituted, and this example is
150~170 DEG C.
The C10 components that rectifying column 212 is obtained are sent to rectifying column 213, isolate C10 isomeries and positive flow silane；
0.05~the 0.15MPa of operating pressure of rectifying column 213, tower top temperature is constituted with operating pressure and tower top
Change and change, this example is 140~165 DEG C.
Above-mentioned rectifying column 203 to the operating pressure and operation temperature of rectifying column 213 is the recommendation of this example,
Not limited to this value.
Third embodiment of the present invention is related to a kind of method for producing simple substance n-alkane.In the present invention the
In three implementation methods, from boiling point elder generation's cutting mode placed in the middle, low boiling mixture and higher boiling mixing are first divided into
Thing, is then separated successively by boiling point height respectively to low boiling mixture and high boiling mixture again.
The preprocessed unit of Fischer-Tropsch synthetic, removal containing C5 isomeries LPG and most C10 with
Upper component, through 11 sets of rectifying columns of rectification cell, be first cut into pentane, C6 isomeries, n-hexane,
C7 isomeries, the mixture of normal heptane and C8 isomeries, normal octane, C9 isomeries, n -nonane, C10 isomeries,
The mixture of positive flow silane, heavy component, then isolate successively respectively pentane, C isomeries, n-hexane,
C7 isomeries, normal heptane and C8 isomeries, normal octane, C9 isomeries, n -nonane, C10 isomeries, positive flow silane,
Heavy constituent, heavy constituent returns to pretreatment unit.
Process chart in present embodiment is as shown in figure 3, specific as follows：
Fischer-Tropsch synthesis oil after will be hydrogenated adds to main fractionating tower 301, is separated into naphtha, light liquids
Paraffin and Paraffin liquid heavy, the operating condition of main fractionating tower 301 are identical with first two implementation method；
The distillate oil of main fractionating tower 301 delivers to distillate oil stabilising arrangement 302, isolate LPG components and
More than C5 stabilization distillate oils, operating condition and the first two implementation method phase of distillate oil stabilising arrangement 302
Together；
Device 302 stabilization naphtha be sent to device 303, isolate pentane, the mixture of C6~C7 with
The mixture of C8~C10, heavy component；0.05~the 0.15MPa of operating pressure of device 303, tower top temperature
Spend and change with the change that operating pressure and tower top are constituted, this example is 50~70 DEG C.
The mixture of pentane, C6~C7 in device 303 is sent to device 304, isolate pentane with
The mixture of C6~C7；0.15~the 0.25MPa of operating pressure of device 304, tower top temperature is pressed with operation
Power and tower top composition change and change, this example be 47~67 DEG C.
The mixture of C6~C7 is sent to device 305 in device 304, isolate C6 isomeries and n-hexane,
The mixture of C7；0.05~the 0.15MPa of operating pressure of device 305, tower top temperature with operating pressure with
And tower top composition change and change, this example be 52~72 DEG C.
The n-hexane of device 305, the mixture of C7 are sent to device 306, isolate n-hexane and C7 components；
0.05~the 0.15MPa of operating pressure of device 306, the change that tower top temperature is constituted with operating pressure and tower top
Change and change, this example is 59~79 DEG C.
The C7 components of device 306 are sent to device 307, isolate normal heptane and C7 isomeries；Device 307
0.05~0.15MPa of operating pressure, tower top temperature becomes with the change that operating pressure and tower top are constituted
Change, this example is 84~104 DEG C.
In addition, C8~C10, the mixture of heavy component are sent to device 308 in device 303, isolate
C8 isomeries and normal octane, C9~C10, the mixture of heavy component.
Essence in the technological process of rectifying column 308 to 313 afterwards, operating condition and first embodiment
Technological process, the operating condition for evaporating tower 108 to 113 are identical, will not be repeated here.
Above-mentioned rectifying column 303 to the operating pressure and operation temperature of rectifying column 313 is the recommendation of this example,
But not limited to this value.
It is pointed out that in the third embodiment, being not limited only to the cutting from the middle of C7 and C8, also
Can first be cut from the middle of any two carbon number.Same reason, can again to cut into it is light,
The mixture of heavy constituent, it is the mixing of isohydrocarbon and normal hydrocarbon under each carbon number to be first cut into according to carbon number
Thing, then by the isolated isohydrocarbon of the mixture and normal hydrocarbon.
It is noted that in actual applications, except using in first embodiment according to component
Boiling point height from low to high or from high to low separate mode successively, it is also possible to using in second embodiment
First it is first cut into being the isohydrocarbon and the mixture of normal hydrocarbon under each carbon number according to carbon number, then this is mixed
The isolated isohydrocarbon of thing and normal hydrocarbon.Low boiling can also be first divided into from boiling point elder generation's cutting mode placed in the middle
Mixture and high boiling mixture, then press boiling point respectively to low boiling mixture and high boiling mixture again
Height is separated successively.It is very flexible and changeable in actual applications.
In addition it is also necessary to explanation is, although be all to obtain six kinds of simple substance N-alkanes in present embodiment
The process system of hydrocarbon, but in actual applications, can be according to the simple substance n-alkane kind number of required acquisition
The quantity of corresponding rectifying column is set.
It will be understood by those skilled in the art that the respective embodiments described above be realize it is of the invention specific
Embodiment, and in actual applications, can to it, various changes can be made in the form and details, without inclined
From the spirit and scope of the present invention.
Claims (9)
1. a kind of method for producing simple substance n-alkane, it is characterised in that comprise the steps of：
Pre-treatment step：It is sequentially placed into Fischer-Tropsch synthetic as raw material in main fractionating tower and stabilizer,
The rectifying under certain pressure and temperature action, obtains stabilization distillate oil；
Rectification step：The stabilization distillate oil is put into rectifying column, under certain pressure and temperature action
Rectifying, obtains the simple substance n-alkane；
Wherein, the species number of the required simple substance n-alkane for obtaining is N kinds, the quantity of the rectifying column
It is 2N-1；The N is any one integer in 1 to 6.
2. it is according to claim 1 production simple substance n-alkane method, it is characterised in that such as
The quantity of really described rectifying column is more than 1, the product separation sequence of each rectifying column include with Types Below it
One, or its any combination：
The first kind, each carbon number is isolated according to the boiling point of product simple substance n-alkane successively from low to high
Under isohydrocarbon and normal hydrocarbon, or isolated successively from high to low often according to product simple substance n-alkane boiling point
Isohydrocarbon and normal hydrocarbon under individual carbon number；
Second Type, from being first cut into weight component between any two kinds of n-alkanes, then respectively for light
The boiling point order of simple substance n-alkane contained by heavy constituent separates isohydrocarbon and positive structure under each carbon number successively
Hydrocarbon；
3rd type, first isolates and is first cut into being the isohydrocarbon and normal hydrocarbon under a certain carbon number according to carbon number
Mixture, then by the isolated isohydrocarbon of the mixture and normal hydrocarbon.
3. it is according to claim 2 production simple substance n-alkane method, it is characterised in that
In the rectification step, the stabilization distillate oil is put into each rectifying column, it is each that acquisition is separated successively
The simple substance n-alkane.
4. it is according to claim 2 production simple substance n-alkane method, it is characterised in that
In the rectification step, the distillate oil is segmented and is cut, obtain each simple substance n-alkane.
5. the method for production simple substance n-alkane according to claim 2, it is characterised in that each
The operating condition of the rectifying column is respectively：
The rectifying column is plate column or packed tower, and the number of theoretical plate of the rectifying column is 20~120, pressure
Power opereating specification 0.05MPa~1.0MPa, 40~200 DEG C of tower top operation temperature, tower reactor operation temperature
60~200 DEG C.
6. it is according to claim 1 production simple substance n-alkane method, it is characterised in that institute
State the subsidiary side line tower of main fractionating tower.
7. it is according to claim 6 production simple substance n-alkane method, it is characterised in that institute
State side line tower M side line of band；The M is 1,2 or 3.
8. it is according to claim 1 production simple substance n-alkane method, it is characterised in that
0.1~the 0.3MPa of operating pressure of the main fractionating tower, 110~140 DEG C of tower top temperature, tower reactor temperature
200~300 DEG C of degree；
1.0~the 2.0MPa of operating pressure of the stabilizer, 110~140 DEG C of tower top temperature, bottom temperature
200~250 DEG C.
9. it is according to claim 1 production simple substance n-alkane method, it is characterised in that institute
The simple substance n-alkane of acquisition is one below or its any combination：
Pentane, n-hexane, normal heptane, normal octane, n -nonane and n-decane.
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| CN107916127A (en) * | 2017-11-03 | 2018-04-17 | 中国科学院山西煤炭化学研究所 | One kind is used for the separated rectification process of Fischer-Tropsch synthetic |
| CN108865245A (en) * | 2017-08-03 | 2018-11-23 | 武汉炼化工程设计有限责任公司 | The method that compound-specific n-alkanes are prepared by Fischer-Tropsch synthetic |
| CN109553505A (en) * | 2017-09-27 | 2019-04-02 | 中国石油天然气股份有限公司 | The method that polyethylene wax by-product lightweight wax oil produces positive flow silane, n-dodecane and n-tetradecane |
| CN109628141A (en) * | 2019-01-29 | 2019-04-16 | 中科合成油技术有限公司 | A method of by F- T synthesis hydrofined oil separating monomer n-alkane |
| CN112391198A (en) * | 2020-10-30 | 2021-02-23 | 中国科学院山西煤炭化学研究所 | Method for continuously separating high-purity n-alkane |
| CN115678600A (en) * | 2022-11-14 | 2023-02-03 | 国家能源集团宁夏煤业有限责任公司 | Preparation method of low-viscosity poly-alpha-olefin lubricating oil |
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| CN108865245B (en) * | 2017-08-03 | 2021-01-12 | 武汉炼化工程设计有限责任公司 | Method for preparing monomer normal alkane from Fischer-Tropsch synthesis product |
| CN109553505A (en) * | 2017-09-27 | 2019-04-02 | 中国石油天然气股份有限公司 | The method that polyethylene wax by-product lightweight wax oil produces positive flow silane, n-dodecane and n-tetradecane |
| CN109553505B (en) * | 2017-09-27 | 2021-09-28 | 中国石油天然气股份有限公司 | Method for producing n-decanone, n-dodecane and n-tetradecane from polyethylene wax byproduct light wax oil |
| CN107916127A (en) * | 2017-11-03 | 2018-04-17 | 中国科学院山西煤炭化学研究所 | One kind is used for the separated rectification process of Fischer-Tropsch synthetic |
| CN107916127B (en) * | 2017-11-03 | 2019-09-10 | 中国科学院山西煤炭化学研究所 | A kind of rectification process for Fischer-Tropsch synthetic separation |
| CN109628141A (en) * | 2019-01-29 | 2019-04-16 | 中科合成油技术有限公司 | A method of by F- T synthesis hydrofined oil separating monomer n-alkane |
| CN112391198A (en) * | 2020-10-30 | 2021-02-23 | 中国科学院山西煤炭化学研究所 | Method for continuously separating high-purity n-alkane |
| CN115678600A (en) * | 2022-11-14 | 2023-02-03 | 国家能源集团宁夏煤业有限责任公司 | Preparation method of low-viscosity poly-alpha-olefin lubricating oil |
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