CN105820838B - A kind of isomerization method for light hydrocarbon - Google Patents
A kind of isomerization method for light hydrocarbon Download PDFInfo
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- CN105820838B CN105820838B CN201510007258.9A CN201510007258A CN105820838B CN 105820838 B CN105820838 B CN 105820838B CN 201510007258 A CN201510007258 A CN 201510007258A CN 105820838 B CN105820838 B CN 105820838B
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Abstract
A kind of isomerization method for light hydrocarbon, light hydrocarbon feedstocks enter de- isopentane tower, overhead stream is drawn as isomerization product, tower base stream contacts progress isomerization reaction with isomerization catalyst into isomerization reactor, reaction product is separated into depentanizer, depentanizer overhead stream introduces de- isopentane tower after being mixed with described light hydrocarbon feedstocks, depentanizer tower base stream introduces deisohexanizer, deisohexanizer overhead stream and tower base stream are drawn as isomerization product, the methylpentane and n-hexane of deisohexanizer lateral line withdrawal function return to isomerization reactor and further converted；Described depentanizer is operated under elevated pressure, described depentanizer overhead stream as the reboiler of described de- isopentane tower thermal source.The method that the present invention is provided makes full use of the condensation heat of depentanizer top gaseous stream in the separation process of positive structure and isoparaffin, effectively the energy consumption of reduction light hydrocarbon isomerization process unit.
Description
Technical field
It is more specifically to one kind that carbon number is less straight the present invention relates to a kind of isomerization method of lighter hydrocarbons
The method that alkane generates branched isoparaffin to improve lighter hydrocarbons octane number by hydroisomerization reaction.
Background technology
With the increasingly enhancing of environmental protection consciousness, requirement of the China to vehicle fuel, particularly gasoline products is increasingly
Strictly, strict limitation is all made that to content of the alkene in gasoline, aromatic hydrocarbons and sulphur etc..Blending group in China's gasoline pool
Dividing has catalytically cracked gasoline, catalytic reforming gasoline, isomerization gasoline and gasoline alkylate etc., and wherein catalytically cracked gasoline is most main
The blending component wanted, but catalytically cracked gasoline has higher alkene and sulfur content, it is easy using hydrogen addition technology Olefin decrease and desulfurization
In causing loss of octane number, therefore, the production capacity for improving other blending components is necessary.In recent years, as crude oil is processed
The raising of ability, the yield increase for being adapted as the naphtha of raw materials for catalytic reforming device is very fast, catalytic reforming unit plus
Work ability has raising by a relatively large margin, but the major part of catalytic reforming generation oil is used for producing aromatic hydrocarbons, and remaining is just as gasoline
Blending component, although catalytic reforming gasoline not olefin-containing and sulphur, its arene content are higher, especially benzene content is easy in blending
In the limits value for reaching gasoline index.It is main that isobutane and butene can be produced using the isoparaffin of carbon eight by alkylated reaction
The gasoline alkylate of composition, gasoline alkylate not olefin-containing, aromatic hydrocarbons and sulphur, are excellent gasoline blending components, but alkylation vapour
The production of oil mainly uses two kinds of techniques of sulfuric acid process and hydrogen fluoride, there is the safety such as equipment corrosion and spent acid processing and environmental protection is asked
Topic, the raising of gasoline alkylate production capacity is restricted.Due to the continuous upgrading of oil quality, with oil hydrogenation it is refined and
Oil product secondary operation device based on being hydrocracked increases, in the hydroprocessing processes of oil product, can produce it is a considerable amount of with
C5 and C6 alkane is the lighter hydrocarbons mainly constituted, because the n-alkane in C5 and C6 alkane has very low octane number, therefore limit
Blending ratio of the lighter hydrocarbons in gasoline pool has been made, n-alkane can be converted into by isomerization reaction by isoparaffin, has been improved
The octane number of lighter hydrocarbons, so as to increase blending ratio of the lighter hydrocarbons in gasoline pool, isomerization gasoline not olefin-containing, aromatic hydrocarbons and
Sulphur, is preferable gasoline blending component, increases isomerization gasoline production, expands blending ratio of the isomerization gasoline in gasoline pool
Example, is the preferable selection for meeting increasingly strict environmental requirement.
Light hydrocarbon isomerization reaction is that in the presence of catalyst, the relatively low light normal paraffin of octane number is converted into octane
The course of reaction of the higher lightweight isoparaffin of value, isomerization reaction is the exothermic reaction controlled by thermodynamical equilibrium, although logical
Cross the higher catalyst of exploitation activity and reduce reaction temperature, can improve total in conversion per pass, but isomerization reaction product
It is that can contain certain density n-alkane, is the octane number of at utmost lifting lighter hydrocarbons, it is necessary to by isomerization reaction product
N-alkane separated with isoparaffin, and make unreacted n-alkane in reaction system interior circulation, improve as far as possible
The isomerization rate of n-alkane.At present, industrially separating positive structure and the method for isoparaffin mainly has adsorption method of separation and rectifying
Method.
Adsorption method of separation is different using characterization of adsorption of the positive structure from isoparaffin on the sorbent, and the two is separated
Process.Isomerization reaction product is separated into logistics and richness rich in n-alkane by being filled with the absorber of adsorbent
Logistics containing isoparaffin, the former returns to isomerization reactor and continues to convert, and the latter is used as isomerization gasoline products.
Rectification method is the process that the difference of separation component boiling point needed for is separated multicomponent, according to required
The different requirements of separation component, set one or more rectifying columns, because tower is simple in construction and control program is easily achieved,
Therefore rectification method is typically to realize one of main method that positive structure is separated with isoparaffin.Due to the positive structure and isomeric alkane in lighter hydrocarbons
Relatively, when the separation accuracy for requiring positive structure and isoparaffin is higher, rectifying column generally requires to set more the boiling point of hydrocarbon
Column plate and use higher reflux ratio, therefore, the energy consumption of rectification method separation process is higher.Using rectification method separate positive structure with
N-alkane is simultaneously recycled back in the light hydrocarbon isomerization technique of reaction member by isoparaffin, although energy consumption needed for distillation process with
Specific separation scheme has close relationship, but would generally account for more than the 60% of device total energy consumption, so using appropriate technique
The energy consumption of means reduction distillation process just can significantly reduce the energy consumption of isomerization unit.
CN101544905A discloses a kind of isomerization method for light hydrocarbon, and light hydrocarbon feedstocks are first through de- isopentane tower separation, tower top
Logistics is drawn as isomerization product, and tower base stream, which enters, occurs isomerization reaction in anterior isomerization reactor, front portion reaction
The outlet streams of device are after gas-liquid separation, and gained liquid phase stream is separated in deisohexanizer, the tower top of deisohexanizer
Logistics and tower base stream are mixed after drawing with the overhead stream of de- isopentane tower, and gasoline stability series are gone collectively as isomerization product
System, the side-stream of deisohexanizer is incorporated into rear portion isomerization reactor, and the reaction stream of rear portion isomerization reactor is through gas
After liquid separation, gained liquid phase stream is all returned and mixed with the liquid phase stream of the gas-liquid separator of anterior isomerization reaction system
Close, collectively as the charging of deisohexanizer.This method has higher normal alkane isomerization rate, wherein C6 N-alkanes alkyl
Originally complete isomerization is realized, and the octane number of light hydrocarbon feedstocks is greatly improved.
In the isomerization method that CN101171212A is proposed, deisohexanizer lateral line withdrawal function thing and permoselective membrane are connect
Touch, obtain what the penetrant fraction that n-hexane and methylpentane concentration improves was improved with methyl cyclopentane and dimethylbutane concentration
Retention fraction, penetrant fraction therein returns to isomerization reactor, and retention fraction is mixed with the logistics of deisohexanizer top
It is used as isomerization gasoline products.Due to being additionally arranged permoselective membrane, while reduction circulation logistics flux, also reduce pair
The requirement of deisohexanizer separation accuracy, deisohexanizer can use relatively low reflux ratio, therefore, significantly reduce isomery
Disguise the energy consumption put.But due to also containing more methylpentane in retention fraction, so that isomerization gasoline products octane
The further raising of value is restricted.
How the normal alkane isomerization rate of light hydrocarbon isomerization reaction unit is being improved, and improve the octane number of light hydrocarbon feedstocks
In the case of, the problem of reduction isomerization process unit energy consumption turns into the urgent need to address at present.
The content of the invention
The technical problem to be solved in the present invention is to provide a kind of isomerization method for light hydrocarbon, normal alkane isomerization is being improved
On the basis of rate, the octane number for improving isomerization gasoline products, while reducing the energy consumption of isomerization process unit.
A kind of isomerization method for light hydrocarbon, light hydrocarbon feedstocks are introduced into de- isopentane tower, and overhead stream draws as isomerization product
Go out, tower base stream introduces isomerization reaction unit, in presence of hydrogen, is contacted with the isomerization catalyst in isomerization reactor
The isomerization reaction of n-alkane is carried out, the product of isomerization reaction unit, which is introduced into depentanizer, to be separated, depentanizer tower top
Obtained C 5 fraction is mixed and introduced into de- isopentane tower, more than the C6 cuts that depentanizer bottom of towe is obtained with described light hydrocarbon feedstocks
Deisohexanizer is introduced, deisohexanizer overhead stream and tower base stream are drawn as isomerization product, described de- isohexane
Logistics of the tower lateral line withdrawal function containing methylpentane and n-hexane returns to described isomerization reaction unit and further converted；Described is de-
Pentanizer is operated under elevated pressure, described depentanizer overhead stream as the reboiler of described de- isopentane tower thermal source.
In the method that the present invention is provided, the operating condition of described isomerization reactor is：Temperature is 100~400 DEG C, table
Sight pressure is 0.5~5.0MPag, and weight (hourly) space velocity (WHSV) is 0.2~10.0h-1, hydrogen/oil mol ratio is 0.05~8.0.
In the method that the present invention is provided, described isomerization catalyst is lived by 0.01~3.0 weight % group VIII metal
Property component and carrier composition；One or more of the described group VIII metal in platinum, palladium, ruthenium and rhodium；Described carrier
For modenite, or the complex carrier that aluminum oxide is constituted with modenite；Preferably, also contain in described complex carrier
β zeolites；Also contain a certain amount of halogen in more preferably described carrier.Wherein the content of metal active constituent is with overall catalyst weight
On the basis of amount, in terms of metal.
Described light hydrocarbon feedstocks are C4~C7 hydrocarbon fractions, and using C5 and C6 alkane as main composition, described lighter hydrocarbons are former
Material comes from hydro-refining unit or hydrocracking unit.
Isomerization method for light hydrocarbon that the present invention is provided has the beneficial effect that：
(1) the isomery C 5 fraction in de- isopentane tower removing light hydrocarbon feedstocks and circulation C 5 fraction is set, isomerization is introduced anti-
Answer in the material that isomerization reaction is carried out in unit and be substantially free of isomery C 5 fraction, the one way of positive structure C 5 fraction can be significantly improved
Conversion ratio, is conducive to improving the utilization ratio of Unit Weight catalyst, saves isomerization catalyst consumption.
(2) depentanizer is set to separate the C 5 fraction in reaction product and be back to de- isopentane tower, it is only different
Structure C 5 fraction is drawn as isomerization gasoline, and positive structure C 5 fraction returns to isomerization reaction unit and proceeds isomerization reaction,
Positive structure C 5 fraction realizes isomerization substantially, and the octane number of isomerization gasoline, which has, greatly to be improved.
(3) deisohexanizer is set further to separate C6 and more than C7 cuts, side line draws methylpentane and n-hexane simultaneously
Return to isomerization reaction unit further to convert, tower top is drawn and is used as isomerization vapour by the logistics mainly constituted of dimethylbutane
Oil product, positive structure C6 cuts realize isomerization substantially, are conducive to producing the isomerization gasoline of higher octane.
(4) operating pressure of depentanizer is higher, and using depentanizer top gaseous stream as de- isopentane bottom of towe again
The thermal source of device is boiled, the condensation heat of depentanizer top gaseous stream is made full use of.In addition, depentanizer is also using the side of heat backflow
Formula, the C 5 fraction that tower top is separated is mixed with hot feed state with light hydrocarbon feedstocks, improves the feeding temperature of de- isopentane tower, drop
The low thermic load of de- isopentane tower bottom reboiler.Substantially the energy consumption of reduction isomerization process unit, reduces isomerization gasoline
Processing cost.
Brief description of the drawings
The schematic flow sheet for the isomerization method for light hydrocarbon that accompanying drawing 1 provides for the present invention.
Embodiment
The present invention is so embodied：
Light hydrocarbon feedstocks are C4~C7 hydrocarbon fractions, and using C5 and C6 alkane as main composition, described light hydrocarbon feedstocks are preferred
Come from hydro-refining unit or hydrocracking unit.Light hydrocarbon feedstocks are the mixture of n-alkane and isoparaffin, according to original
Expect the difference in source, the ratio of positive structure and isoparaffin is changed greatly, the isomerization that usual oil product time processing process is produced is former
N-alkane proportion is larger in material, and isoparaffin proportion in the isomerate feeds that oil product secondary processing process is produced
It is larger.
Light hydrocarbon feedstocks initially enter de- isopentane tower, and the isomery C 5 fraction in light hydrocarbon feedstocks is separated and isomery is used as
Change a part for gasoline, tower base stream is described to remove isomery C5 light hydrocarbon feedstocks, including C5 n-alkanes and more than C6 alkane
More than C6 alkane include C6 alkane and a small amount of C7 alkane.The operating condition of de- isopentane tower is：The apparent pressure of tower top is
0.10~0.40MPag, tower top temperature is 60~70 DEG C, and column bottom temperature is 88~100 DEG C, and tower reflux ratio (R/D) is 5~10.It is de-
Except isomery C5 light hydrocarbon feedstocks enter isomerization reaction unit.
Isomerization reaction unit is provided with feed pump, heat exchanger, reaction heating furnace, isomerization reactor, gas-liquid separator, hydrogen
The equipment such as air compressor, wherein isomerization reactor are loaded in the key equipment of isomerization reaction unit, isomerization reactor
There is isomerization catalyst.Isomerization reaction is reacted for slight exotherm, although the fuel factor of reaction is little, but reaction temperature is aligned
The equilibrium conversion influence of structure alkane is larger, for preferably controlling reaction temperature, preferably by the catalysis in isomerization reactor
Agent bed is divided into 2~3 sections or using 2~3 reactors, between adjacent two-stage catalytic agent bed or two adjacent reactors it
Between fill into the relatively low cold medium of temperature, make reaction temperature control in required scope.
In the method that the present invention is provided, the isomerization catalyst of filling is by 0.01~3.0 weight %'s in isomerization reactor
Group VIII metal active component and carrier composition；One or more of the described group VIII metal in platinum, palladium, ruthenium and rhodium；
Described carrier is the modenite complex carrier that either aluminum oxide is constituted with modenite.Preferably, described compound load
Also contain β zeolites in body；Also contain a certain amount of halogen in more preferably described carrier.The content of wherein metal active constituent is
On the basis of total catalyst weight, the content in terms of metal.
The operating condition of described isomerization reactor is：Temperature be 100~400 DEG C, apparent pressure be 0.5~
5.0MPag, weight (hourly) space velocity (WHSV) is 0.2~10.0h-1, hydrogen/oil mol ratio is 0.05~8.0.
Described isomerization reaction unit also includes isomerization reaction product systems stabilisation, generally by stabilizer and correlation
Equipment is constituted, and is removed the hydrogen that dissolves in isomerization reaction product by systems stabilisation and micro is generated by cracking side reaction
C1~C3 low-carbon alkanes.
Isomerization reaction product after stable processing enters to be separated in depentanizer, and depentanizer tower top is obtained
C 5 fraction the de- isopentane tower of introducing is mixed with isomerate feeds, more than the C6 cuts that bottom of towe is obtained are introduced into deisohexanizer
Row separation.Described depentanizer is operated under pressure, and the apparent pressure of tower top is 0.80~1.20MPag, it is preferable that
The operating condition of described depentanizer is：The apparent pressure of tower top is 0.80~1.10MPag, and tower top temperature is 115~125 DEG C,
Bottom temperature is 150~175 DEG C.
The key component of deisohexanizer overhead stream is dimethylbutane, is drawn as isomerization gasoline products, is taken off different
The tower base stream of hexane tower is that more than C7 cuts also serve as the extraction of isomerization gasoline, and described more than C7 cuts are mainly C7 hydrocarbon
Class, the lateral line withdrawal function logistics of deisohexanizer returns to isomerization reaction unit and entered using methylpentane and normal hexane as main composition
One step is converted.The operating condition of described deisohexanizer is：The apparent pressure of tower top is 0.1~0.5MPag, and tower top temperature is 70
~130 DEG C, bottom temperature is 100~170 DEG C.
In the method that the present invention is provided, described depentanizer uses higher operating pressure, and using the side of heat backflow
Formula, the C 5 fraction that tower top is separated is without further cooling, but it is de- different that feeding is mixed with light hydrocarbon feedstocks with hot feed state
Pentanizer, improves the feeding temperature of de- isopentane tower.In addition, the potential temperature of depentanizer overhead stream meets de- isopentane tower again
Boil device thermal source potential temperature requirement, can as the reboiler of described de- isopentane tower thermal source.Described de- isopentane tower bottom of towe
Reboiler small part deficiency heat is provided by other thermals source.The method that the present invention is provided makes the condensation of depentanizer top gaseous stream
Heat is fully used, and to take off most of heat needed for isopentane tower provides separation, significantly reduces de- isopentane bottom of towe again
The thermic load of device is boiled, the energy consumption of light hydrocarbon isomerization process unit is effectively reduced.
Further illustrate and only indicated mainly in the isomerization method for light hydrocarbon that the present invention is provided, accompanying drawing below in conjunction with the accompanying drawings
Equipment, eliminates auxiliary equipment, instrument and valve etc., but not thereby limiting the invention.
The schematic flow sheet for the isomerization method for light hydrocarbon that accompanying drawing 1 provides for the present invention, as shown in figure 1, light hydrocarbon feedstocks are through pipe
Line 1 introduces isomerization unit, and the C 5 fraction isolated with the depentanizer 18 through pipeline 10 is mixed, and introduces de- different through pipeline 2
Pentanizer 16.The separation of isomery C 5 fraction and positive structure C5 and heavier fraction is carried out in de- isopentane tower 16.With isomery C5 alkane
Gaseous stream mainly to constitute is drawn through pipeline 3 and sent as isomerization gasoline products by the Base top contact of de- isopentane tower 16
Go out device.After de- isopentane bottom of towe liquid phase stream passes via line 4 is mixed with the circulation C6 cuts from pipeline 13, sent into through pipeline 5
Isomerization reaction unit 17, carries out the isomerization reaction of n-alkane, isomerization reaction product in isomerization reaction unit 17
Enter depentanizer 18 through pipeline 6, carry out the separation of C 5 fraction and more than C6 cuts.The C 5 fraction gas phase at the top of depentanizer 18
Stream passes via line 7 enters de- isopentane tower bottom reboiler 15, after the C 5 fraction condensed through tower bottom reboiler 15 is drawn through pipeline 8,
Without further cooling, light hydrocarbon feedstocks mixing of the part through pipeline 10 and pipeline 1 enters de- isopentane tower through pipeline 2
16, another part returns to depentanizer 18 as overhead reflux through pipeline 9.The bottom of towe C6 above cuts of depentanizer 18 are through pipeline
11 introduce deisohexanizer 19, are drawn by the overhead stream mainly constituted of dimethylbutane by pipeline 12, are used as isomerization vapour
A part for oil product, is drawn by the tower base stream mainly constituted of more than C7 cuts by pipeline 14, also serves as isomerization gasoline
A part, the side-stream of deisohexanizer 19, main composition is methylpentane and n-hexane, is drawn by pipeline 13 and pipeline
De- isomery C 5 fraction mixing in 4, returns to isomerization reaction unit 17, is further converted to the higher dimethyl butyrate of octane number
Alkane.
The present invention is further illustrated by the following examples.
Embodiment 1
Embodiment 1 is using the process scheme shown in accompanying drawing 1, and the process scale of isomerization unit is 300,000 tons/year.It is different
Structure raw material is the lighter hydrocarbons by hydrofinishing, in addition to containing C5 and C6 alkane, also containing a small amount of other components, its specific group
Into data as shown in table 1, as can be seen from Table 1：The molar content of C5 alkanes is 47.94% in raw material, and wherein isopentane is accounted for
The 42.49% of C5 paraffinicities；The molar content of C6 alkanes is 39.93%, and wherein dimethylbutane accounts for C6 alkanes and contained
The 7.29% of amount.The research octane number (RON) of raw material is 67.5.The composition and property of isomerization gasoline products are also shown in Table 1 below, from
Table 1 can be seen that：The content that isopentane in isomerization gasoline products accounts for C5 alkanes has brought up to 95.15%, dimethyl butyrate
The content that alkane accounts for C6 alkanes has brought up to 48.58%, and the research octane number (RON) of isomerization gasoline products has brought up to 86.9.
Table 2 lists the operating condition of de- isopentane tower, depentanizer and deisohexanizer.The apparent pressure of de- isopentane tower top
Power is 0.2MPag, and bottom of towe liquidus temperature is 93 DEG C；The apparent pressure in depentanizer top is 0.9MPag, and top gaseous phase temperature is 127
DEG C, it is higher than de- isopentane bottom of towe liquidus temperature 34 DEG C, it is suitable as the thermal source of the reboiler of de- isopentane tower.
Using the present embodiment process program when, take off the energy needed for isopentane tower, depentanizer and deisohexanizer separation
Consumption accounts for the 80% of device total energy consumption, therefore, and the energy of isomerization unit can be just greatly lowered in the thermic load of three towers of reduction
Consumption.The thermic load of the reboiler of three towers is as shown in table 3, as shown in Table 3：Depentanizer top gas is supplied to the heat of de- isopentane tower to bear
Lotus is 7749kW, accounts for the 24.94% of three tower total heat duties.The total heat duties that three towers need outer supplying heat source to provide are 23326kW.
Embodiment 2
Embodiment 2 is also using the process scheme shown in accompanying drawing 1, except that the gas gas-phase objects that depentanizer top is drawn
Stream is using the conventional condensation type of cooling.
The isomerate feeds of embodiment 2 are identical with the raw material of embodiment 1, the process conditions of the two isomerization reaction part
It is identical, and the separation accuracy of de- isopentane tower, depentanizer and deisohexanizer is also identical.
The operating condition that isopentane tower, depentanizer and deisohexanizer are taken off in embodiment 2 is as shown in table 2, and three towers are again
The thermic load for boiling device is as shown in table 3.Due to that need not consider the potential temperature problem of depentanizer top gas phase, depentanizer can be relatively low
Pressure under operate.
The total heat duties of de- isopentane tower, depentanizer and the outer supplying heat source offer of deisohexanizer need are in embodiment 2
30871kW, 32.35% is added compared with the total heat duties in embodiment 1.
Table 1
| Isomerate feeds | Isomerization gasoline products | |
| Mole composition, % | ||
| Iso-butane | 0.43 | 0.46 |
| Normal butane | 5.12 | 5.26 |
| Isopentane | 20.37 | 46.47 |
| Pentane | 27.57 | 2.37 |
| Pentamethylene | 1.96 | 2.02 |
| 2,2- dimethylbutanes | 0.36 | 14.55 |
| 2,3- dimethylbutanes | 2.55 | 4.23 |
| 2- methylpentanes | 12.74 | 9.96 |
| 3- methylpentanes | 8.71 | 4.94 |
| N-hexane | 15.57 | 4.98 |
| Methyl cyclopentane | 1.18 | 2.57 |
| Hexamethylene | 3.30 | 0.00 |
| Benzene | 0.15 | 2.19 |
| Heptane | 0.00 | 0.00 |
| It is total | 100.00 | 100.00 |
| Research octane number (RON) | 67.5 | 86.9 |
Table 2
Table 3
Claims (10)
1. a kind of isomerization method for light hydrocarbon, it is characterised in that light hydrocarbon feedstocks enter de- isopentane tower, the isomery C5 that tower top is obtained evaporates
It is allocated as drawing for isomerization product, positive structure C5 and more than the C6 cuts that bottom of towe is obtained enter isomerization reaction unit, deposit in hydrogen
Under, the isomerization reaction for carrying out n-alkane, isomerization reaction list are contacted with the isomerization catalyst in isomerization reactor
The product of member is separated into depentanizer, and depentanizer overhead stream introduces de- isoamyl after being mixed with described light hydrocarbon feedstocks
Alkane tower, more than the C6 cuts that depentanizer bottom of towe is obtained introduce deisohexanizer, deisohexanizer overhead stream and tower base stream
Drawn as isomerization product, described logistics of the deisohexanizer lateral line withdrawal function containing methylpentane and n-hexane returns described
Isomerization reaction unit is further converted；Described depentanizer is operated under elevated pressure, and described depentanizer overhead stream is made
For the thermal source of the reboiler of described de- isopentane tower.
2. according to the method for claim 1, it is characterised in that the operating condition of described isomerization reactor is：Temperature is 100
~400 DEG C, apparent pressure is 0.5~5.0MPag, and weight (hourly) space velocity (WHSV) is 0.2~10.0h-1, hydrogen/oil mol ratio is 0.05~8.0.
3. according to the method for claim 1, it is characterised in that described isomerization catalyst is by the of 0.01~3.0 weight %
Group VIII metal active component and carrier composition, the one kind or several of described group VIII metal in platinum, palladium, ruthenium and rhodium
Kind；Described carrier be modenite, or aluminum oxide and modenite complex carrier.
4. according to the method for claim 1, it is characterised in that the operating condition of described de- isopentane tower is：The apparent pressure of tower top
Power is 0.1~0.4MPag, and tower top temperature is 60~70 DEG C, and column bottom temperature is 88~100 DEG C, and reflux ratio is 5~10.
5. according to the method for claim 1, it is characterised in that the operating condition of described depentanizer is：The apparent pressure of tower top
For 0.80~1.20MPag, tower top temperature is 115~125 DEG C, and bottom temperature is 150~175 DEG C.
6. according to the method for claim 1, it is characterised in that described deisohexanizer overhead stream evaporates for dimethylbutane
Point, described deisohexanizer tower base stream is more than C7 cuts.
7. according to the method for claim 6, it is characterised in that the operating condition of described deisohexanizer is：The apparent pressure of tower top
Power is 0.1~0.5MPa, and tower top temperature is 70~130 DEG C, and bottom temperature is 100~170 DEG C.
8. according to the method for claim 1, it is characterised in that the catalyst of filling is divided into 2~3 in described isomerization reactor
Section bed, fills into the temperature that the relatively low cold medium of temperature adjusts reaction stream between adjacent two sections of beds.
9. according to the method for claim 1, it is characterised in that described isomerization reactor is by 2~3 reactor groups connected
Into filling into the temperature that the relatively low cold medium of temperature adjusts reaction stream between two neighboring reactor.
10. according to the method for claim 1, it is characterised in that described light hydrocarbon feedstocks are C4~C7 hydrocarbon fractions, and with C5 and
C6 alkane is main composition.
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| US11414361B2 (en) * | 2017-08-28 | 2022-08-16 | Sabic Global Technologies B.V. | Systems and methods for converting n-butane to iso-butane |
| CN110669550B (en) * | 2018-07-03 | 2021-11-12 | 中国石油化工股份有限公司 | Isomerization method of aromatic raffinate oil |
| CN110903851B (en) * | 2018-09-14 | 2022-03-11 | 中国石油化工股份有限公司 | C5-C6Light hydrocarbon isomerization method |
| CN109608299B (en) * | 2018-12-13 | 2021-09-21 | 华南理工大学 | Petroleum light hydrocarbon separation device and method based on inter-tower heat integration technology |
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