CN108046974A - A kind of Separation of Benzene, hexamethylene, the system and method for cyclohexene - Google Patents
A kind of Separation of Benzene, hexamethylene, the system and method for cyclohexene Download PDFInfo
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- CN108046974A CN108046974A CN201711480168.7A CN201711480168A CN108046974A CN 108046974 A CN108046974 A CN 108046974A CN 201711480168 A CN201711480168 A CN 201711480168A CN 108046974 A CN108046974 A CN 108046974A
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- extractive distillation
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- cyclohexene
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 127
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 125000004836 hexamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 title claims abstract description 38
- 238000000926 separation method Methods 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims description 28
- 238000000895 extractive distillation Methods 0.000 claims abstract description 63
- 238000000605 extraction Methods 0.000 claims abstract description 42
- 238000007599 discharging Methods 0.000 claims abstract description 19
- 125000000596 cyclohexenyl group Chemical group C1(=CCCCC1)* 0.000 claims abstract description 3
- 238000010992 reflux Methods 0.000 claims description 18
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 15
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 11
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 10
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 claims description 9
- 229940113088 dimethylacetamide Drugs 0.000 claims description 8
- 238000001704 evaporation Methods 0.000 claims description 4
- YEJRWHAVMIAJKC-UHFFFAOYSA-N 4-Butyrolactone Chemical compound O=C1CCCO1 YEJRWHAVMIAJKC-UHFFFAOYSA-N 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 239000002608 ionic liquid Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- LCEDQNDDFOCWGG-UHFFFAOYSA-N N-Formyl-Morpholine Natural products O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 150000002825 nitriles Chemical class 0.000 claims 1
- 238000011084 recovery Methods 0.000 description 17
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 9
- HUMNYLRZRPPJDN-UHFFFAOYSA-N benzaldehyde Chemical compound O=CC1=CC=CC=C1 HUMNYLRZRPPJDN-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000013329 compounding Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 2
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000036571 hydration Effects 0.000 description 2
- 238000006703 hydration reaction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000012046 mixed solvent Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- QNGNSVIICDLXHT-UHFFFAOYSA-N para-ethylbenzaldehyde Natural products CCC1=CC=C(C=O)C=C1 QNGNSVIICDLXHT-UHFFFAOYSA-N 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 235000011037 adipic acid Nutrition 0.000 description 1
- 239000001361 adipic acid Substances 0.000 description 1
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 150000003951 lactams Chemical class 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
Classifications
-
- 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
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention discloses a kind of Separation of Benzene, hexamethylene, the system of cyclohexene, including sequentially connected first extractive distillation column (1), the second extractive distillation column (2) and rectifying column (3)；The middle part of first extractive distillation column (1) has feedstock pipeline (5), top has extractant feed pipeline first (41), top has hexamethylene extraction pipeline (8), bottom has tower bottoms discharging pipeline first (6), leads to the second extractive distillation column (2) and is used as its feeding line；The top of second extractive distillation column (2) has extractant feed pipeline second (42), top has benzene extraction pipeline (9), bottom has tower bottoms discharging pipeline second (7), leads to rectifying column (3) and is used as its feeding line；There is cyclohexene extraction pipeline (10) at the top of rectifying column (3), bottom has extractant discharging pipeline (4), separates Liang Ge branches as the extractant feed pipeline first (41) and the extractant feed pipeline second (42).
Description
Technical field
The present invention relates to the organic separation technology field of chemical industry more particularly to a kind of Separation of Benzene, hexamethylene, cyclohexene system
And method.
Background technology
Partial hydrogenation of benzene prepares cyclohexene, cyclohexene hydration method prepares cyclohexanol, cyclohexene hydration method prepares adipic acid, oneself
In the Chemical Manufactures unit such as lactams, the separation of benzene, hexamethylene, cyclohexene is a necessary operation.But these three substances boil
Point is close, and benzene and hexamethylene, benzene and cyclohexene can form azeotropic mixture, mainly be separated at present by extraction fractional distillation.
But the separation process of benzene, hexamethylene, cyclohexene, mostly using four-column process flow, energy consumption is larger or extraction is smart
Deethanizer design is evaporated for next door tower, but pipeline designs are still complicated, operating difficulties.Patent CN10261726A gives typical four
Tower flow and next door tower technology, and propose that four new towers or five tower flows, invention main purpose are energy saving.But the hair
Free flow journey is still complicated, takes up an area greatly, and equipment installation is more, and maintenance is difficult.Therefore, it is necessary to the simple Separation of Benzene of development process, rings
The system and method for hexane, cyclohexene, to reduce the investment of equipment place, while energy-saving and emission-reduction.
The content of the invention
In view of problems of the prior art, it is an object of the invention to provide a kind of Separation of Benzene, hexamethylene, cyclohexene
System and method, purify out purity>Benzene, hexamethylene, the cyclohexene product of 99.5wt%, while simplification of flowsheet, subtract
Few equipment and place investment, effective energy-saving and emission-reduction.
For this purpose, the present invention adopts the following technical scheme that：
In a first aspect, the present invention provides a kind of Separation of Benzene, hexamethylene, the system of cyclohexene, the system comprises connect successively
The first extractive distillation column (1), the second extractive distillation column (2) and the rectifying column (3) connect；Wherein：
The middle part of first extractive distillation column (1) has feedstock pipeline (5), and top has extractant feed pipeline first
(41), top has hexamethylene extraction pipeline (8), and bottom has tower bottoms discharging pipeline first (6), leads to the second extracting rectifying
The middle part of tower (2) is as the second extractive distillation column (2) feeding line；
The top of second extractive distillation column (2) has extractant feed pipeline second (42), and there is benzene to produce pipeline at top
(9), bottom has tower bottoms discharging pipeline second (7), leads to feeding line of the middle part of rectifying column (3) as rectifying column (3)；
There is cyclohexene extraction pipeline (10), bottom has extractant discharging pipeline (4), separates at the top of rectifying column (3)
Liang Ge branches are as the extractant feed pipeline first (41) and the extractant feed pipeline second (42).
Preferably, the inside of first extractive distillation column (1), the second extractive distillation column (2) and rectifying column (3) is filled with
High Efficient Standard Packing.
Second aspect, the present invention provides a kind of Separation of Benzene, hexamethylene, cyclohexene method, the method utilize basis
System described in first aspect present invention carries out, and includes the following steps：
(1) raw material containing benzene, hexamethylene, cyclohexene is added in into the first extractive distillation column through feedstock pipeline (5)
(1), extractant while through the extractant feed pipeline first (41) on the first extractive distillation column (1) top is added in, carries out first
Secondary extracting rectifying, tower top produce product hexamethylene through hexamethylene extraction pipeline (8)；
The tower bottoms of (2) first extractive distillation columns (1) leads to the second extractive distillation column through tower bottoms discharging pipeline first (6)
(2) middle part is fed as the second extractive distillation column (2), while through the extractant feed pipeline second (42) in the second extraction essence
It evaporates tower (2) top and is passed through extractant, carry out second of extracting rectifying, tower top produces products benzene through benzene extraction pipeline (9)；
The tower bottoms of (3) second extractive distillation columns (2) leads to the middle part of rectifying column (3) through tower bottoms discharging pipeline second (7)
It is fed as rectifying column (3), carries out rectification process, tower top produces product cyclohexene, tower reactor warp through cyclohexene extraction pipeline (10)
Extractant discharging pipeline (4) produces extractant, so separate Liang Ge branches as the extractant feed pipeline first (41) and
The extractant feed pipeline second (42) is back to first extractive distillation column (1) and the second extractive distillation column (2) respectively
The recycling of extractant is realized on top.
Wherein, the extractant includes being selected from：
DMAC N,N' dimethyl acetamide (DMAC), N- N-formyl morpholine Ns (NMF), dimethylformamide (DMF), gamma-butyrolacton, oneself
Any one in dintrile, ionic liquid；With,
N-Methyl pyrrolidone (NMP)；With,
Sulfolane；
Wherein, the weight percent of the extractant sulfolan be 50~90wt%, such as 50wt%, 57wt%,
60wt%, 65wt%, 68wt%, 70wt%, 75wt%, 78wt%, 80wt%, 85wt%, 88wt% or 90wt%；The N-
The weight percent of methyl pyrrolidone be 5~45wt%, such as 5wt%, 8wt%, 10wt%, 12wt%, 15wt%,
18wt%, 20wt%, 25wt%, 30wt%, 35wt%, 40wt% or 45wt%.
Be preferably added to the mass ratio of extractant in first extractive distillation column and the raw material for (1~
5):1, such as 1:1、1.5:1、2:1、2.2:1、2.5:1、2.8:1、3:1、3.2:1、3.5:1、3.8:1、4:1、4.2:1、4.5:
1、4.8:1、5:1；The mass ratio of the extractant being added in second extractive distillation column and the raw material is (1~5):1,
Such as 1:1、1.5:1、2:1、2.2:1、2.5:1、2.8:1、3:1、3.2:1、3.5:1、3.8:1、4:1、4.2:1、4.5:1、
4.8:1、5:1 etc..
Preferably, 1~2MPa of pressure of first extractive distillation column, for example, 1Mpa, 1.1Mpa, 1.2Mpa, 1.3Mpa,
1.4Mpa, 1.5Mpa, 1.6Mpa, 1.7Mpa, 1.8Mpa, 1.9MPa or 2MPa, column bottom temperature are 140~180 DEG C, tower top temperature
For 80~110 DEG C；The pressure of second extractive distillation column be 1~2MPa, such as 1Mpa, 1.1Mpa, 1.2Mpa, 1.3Mpa,
1.4Mpa, 1.5Mpa, 1.6Mpa, 1.7Mpa, 1.8Mpa, 1.9MPa or 2MPa, column bottom temperature are 240~280 DEG C, tower top temperature
For 80~110 DEG C；The pressure of the rectifying column is 1~2MPa, and column bottom temperature is 240~280 DEG C, and tower top temperature is 80~110
℃。
Preferably, the reflux ratio of first extractive distillation column be 0.1~2, such as 0.1,0.5,0.7,1,1.2,1.5,
1.7 or 2, preferably 0.5~1.5；The reflux ratio of second extractive distillation column be 1~10, such as 1,1.5,2,2.6,3,4,5,
5.5th, 6,6.5,6,6.5,7,7.5,8,8.7,9,9.6 or 10, preferably 2~6；The reflux ratio of the rectifying column is 1~10, example
Such as 1,1.5,2,2.6,3,4,5,5.5,6,6.5,6,6.5,7,7.5,8,8.7,9,9.6 or 10, preferably 4~8.
Compared with prior art, the present invention at least has the advantages that：
1st, system provided by the present invention can disposably purify out purity>Hexamethylene, benzene and the cyclohexene production of 99.5wt%
Product, the rate of recovery are more than 99%,；
2nd, extractant effect of extracting is good, preparation is simple, solvent recovering rate is high, regeneration energy consumption is low；
3rd, industrial hexamethylene, cyclohexene, separated four tower of benzene, five tower flows are effectively reduced to three tower streams by the present invention
Journey, it is energy-saving, save space and equipment investment.
4th, the present invention changes traditional separation sequence, it is disposable using three towers directly isolate successively hexamethylene, benzene and
Cyclohexene overcomes mixed solvent in the prior art so that benzene is easy to separate from hexamethylene and cyclohexene mixture and causes ring
The prejudice that hexane and cyclohexene separating difficulty increase.
5th, this method uses same mixed extractant, by adjusting the solvent ratio of different towers, reaches separation different material
Purpose, it is easy to operate, effect protrude.
Description of the drawings
Fig. 1 is the Separation of Benzene of the present invention, the flow chart of the system of hexamethylene, cyclohexene.
Reference numeral meaning is as follows in figure：
The first extractive distillation columns of 1-；The second extractive distillation columns of 2-；3- rectifying columns；4- extractants discharging pipeline；41- extractants
Feeding line first；42- extractant feed pipeline second；5- feedstock pipelines；6- tower bottoms discharging pipeline first；7- tower bottoms discharges
Pipeline second；8- hexamethylenes produce pipeline；9- benzene produces pipeline；10- cyclohexene produces pipeline.
Specific embodiment
Technical solution to further illustrate the present invention below with reference to the accompanying drawings and specific embodiments.But following reality
Example is only the simple example of the present invention, does not represent or limit the scope of the present invention, protection scope of the present invention
It is subject to claims.
Embodiment 1
A kind of Separation of Benzene, hexamethylene, the system of cyclohexene, as shown in Figure 1, including the first sequentially connected extracting rectifying
Tower, the second extractive distillation column and rectifying column, the first extractive distillation column and the second extractive distillation column tower top be equipped with extractant into
Expects pipe line, rectifying tower bottom are connected equipped with extractant recovery channel with the extractant suction line of two towers, the first extraction essence
The inside for evaporating tower, the second extractive distillation column and rectifying column is filled with High Efficient Standard Packing.
Using above system from certain 100,000 tons/year of cyclohexanone production apparatus Separation of Benzene, hexamethylene, cyclohexene, step is such as
Under：
(1) the first extractive distillation column will be added in containing the raw material of benzene, hexamethylene, cyclohexene, while through extractant feed pipe
Line first adds in extractant into the first extractive distillation column, carries out first time extracting rectifying, tower pressure interior force 1.4MPa, and column bottom temperature is
160 DEG C, tower top temperature is 90 DEG C；Reflux ratio is 0.5；Wherein, the extractant include n,N-dimethylacetamide (DMAC) with
The mixed solvent that N-Methyl pyrrolidone (NMP) and sulfolane compounding form, the proportion of sulfolane described in extractant are
The proportion of 60wt%, NMP are 30wt%；The mass ratio of the extractant of addition and the raw material is 3:1, overhead extraction product ring
Hexane, purity 99.6wt%, the rate of recovery 99.02%；
The tower bottoms of (2) first extractive distillation columns is carried out through tower bottoms discharging pipeline first into the second extractive distillation column middle part
Second of rectifying extracts, while extractant, tower pressure interior force are added in into the second extractive distillation column through extractant feed pipeline second
1.4MPa, column bottom temperature are 260 DEG C, and tower top temperature is 90 DEG C, reflux ratio 2；The quality of the extractant of addition and the raw material
The ratio between be 4:1, overhead extraction products benzene, purity 99.7wt%, the rate of recovery 99.17%；
The tower bottoms of (3) second extractive distillation columns enters rectifying column through tower bottoms discharging pipeline second and is separated, rectifying column
Pressure for 1.5MPa, column bottom temperature is 267 DEG C, and tower top temperature is 85 DEG C, reflux ratio 4；The matter of extractant and the raw material
The ratio between amount is 1:1, overhead extraction product cyclohexene, purity 99.8wt%, the rate of recovery 99.15%, tower reactor extraction extractant,
It is back to the first extractive distillation column and the second extractive distillation column respectively.
Embodiment 2
System is same as Example 1, and method is similar, unlike：
The composition of extractant is：Gamma-butyrolacton and the mixing that N-Methyl pyrrolidone (NMP) and sulfolane compounding form are molten
Agent, the proportion of sulfolane described in extractant is 90wt%, and the proportion of NMP is 5wt%；First extractive distillation column reflux ratio is
1.5, overhead extraction product hexamethylene, purity 99.7wt%, the rate of recovery 99.13%；
Second extractive distillation column reflux ratio is 6, and the products benzene purity of top of tower extraction is 99.6w%, and the rate of recovery is
99.25%；Rectifier column reflux ratio is 8, and the cyclohexene product purity of overhead extraction is 99.8wt%, the rate of recovery 99.31%.
Embodiment 3
System is same as Example 1, and method is similar, unlike：
The composition of extractant is：Ionic liquid and the mixing that N-Methyl pyrrolidone (NMP) and sulfolane compounding form are molten
Agent, the proportion of sulfolane described in extractant is 80wt%, and the proportion of NMP is 10wt%；First extractive distillation column reflux ratio is
1.1, overhead extraction product hexamethylene, purity 99.8wt%, the rate of recovery 99.24%；
Second extractive distillation column reflux ratio is 4, and the products benzene purity of top of tower extraction is 99.7w%, and the rate of recovery is
99.25%；Rectifier column reflux ratio is 6, and the cyclohexene product purity of overhead extraction is 99.7wt%, the rate of recovery 99.37%.
Comparative example 1
With differing only in for embodiment 1：Extractant replaces with repefral.
The cyclohexane product purity of first extracting rectifying top of tower extraction is 63wt%, the rate of recovery 71%；
The benzaldehyde product purity of second extracting rectifying top of tower extraction is 67wt%, the rate of recovery 53%；
The cyclohexene product purity of extraction is 64wt% at the top of rectifying column, the rate of recovery 68%.
Comparative example 2
With differing only in for embodiment 1：Extractant replaces with DMAC.
The cyclohexane product purity of first extracting rectifying top of tower extraction is 83wt%, the rate of recovery 77%；
The benzaldehyde product purity of second extracting rectifying top of tower extraction is 73wt%, the rate of recovery 81%；
The cyclohexene product purity of extraction is 61wt% at the top of rectifying column, the rate of recovery 69%.
The present invention illustrates the detailed process equipment of the present invention and technological process by above-described embodiment, but the present invention is not
Above-mentioned detailed process equipment and technological process are confined to, that is, does not mean that the present invention has to rely on above-mentioned detailed process equipment and work
Skill flow could be implemented.Person of ordinary skill in the field is it will be clearly understood that any improvement in the present invention, to product of the present invention
The equivalence replacement of each raw material and the addition of auxiliary element, the selection of concrete mode etc., all fall within protection scope of the present invention and public affairs
Within the scope of opening.
Claims (8)
1. the system of a kind of Separation of Benzene, hexamethylene, cyclohexene, which is characterized in that the system comprises the sequentially connected first extractions
Take rectifying column (1), the second extractive distillation column (2) and rectifying column (3)；Wherein：
The middle part of first extractive distillation column (1) has feedstock pipeline (5), and top has extractant feed pipeline first (41),
Top has hexamethylene extraction pipeline (8), and bottom has tower bottoms discharging pipeline first (6), leads to the second extractive distillation column (2)
Middle part as the second extractive distillation column (2) feeding line；
The top of second extractive distillation column (2) has extractant feed pipeline second (42), and top has benzene extraction pipeline (9), bottom
Portion has tower bottoms discharging pipeline second (7), leads to feeding line of the middle part of rectifying column (3) as rectifying column (3)；
There is cyclohexene extraction pipeline (10), bottom has extractant discharging pipeline (4), separates two at the top of rectifying column (3)
Branch is as the extractant feed pipeline first (41) and the extractant feed pipeline second (42).
2. the system of Separation of Benzene according to claim 1, hexamethylene, cyclohexene, which is characterized in that the first extraction essence
The inside for evaporating tower (1), the second extractive distillation column (2) and rectifying column (3) is filled with High Efficient Standard Packing.
3. a kind of method of Separation of Benzene, hexamethylene, cyclohexene, which is characterized in that the method is using according to claim 1
System carry out, include the following steps：
(1) raw material containing benzene, hexamethylene, cyclohexene is added in into the first extractive distillation column (1) through feedstock pipeline (5), together
Extractant feed pipeline first (41) described in Shi Jing adds in extractant on the first extractive distillation column (1) top, carries out first time extraction
Rectifying, tower top produce product hexamethylene through hexamethylene extraction pipeline (8)；
The tower bottoms of (2) first extractive distillation columns (1) leads to the second extractive distillation column (2) through tower bottoms discharging pipeline first (6)
Middle part is fed as the second extractive distillation column (2), while through the extractant feed pipeline second (42) in the second extractive distillation column
(2) top is passed through extractant, carries out second of extracting rectifying, and tower top produces products benzene through benzene extraction pipeline (9)；
The tower bottoms of (3) second extractive distillation columns (2) leads to the middle part conduct of rectifying column (3) through tower bottoms discharging pipeline second (7)
Rectifying column (3) is fed, and carries out rectification process, and tower top produces product cyclohexene through cyclohexene extraction pipeline (10), and tower reactor is through extraction
Agent discharging pipeline (4) produces extractant, and then separates Liang Ge branches as the extractant feed pipeline first (41) and described
Extractant feed pipeline second (42) is back to the upper of first extractive distillation column (1) and the second extractive distillation column (2) respectively
Portion realizes the recycling of extractant.
4. the method for Separation of Benzene according to claim 3, hexamethylene, cyclohexene, which is characterized in that the extractant includes
It is selected from：
DMAC N,N' dimethyl acetamide (DMAC), N- N-formyl morpholine Ns (NMF), dimethylformamide (DMF), gamma-butyrolacton, oneself two
Any one in nitrile, ionic liquid；With,
N-Methyl pyrrolidone (NMP)；With,
Sulfolane；
Wherein, the weight percent of the extractant sulfolan be 50~90wt%, the weight of the N-Methyl pyrrolidone
Percentage is 5~45wt%.
5. Separation of Benzene, hexamethylene, the method for cyclohexene according to claim 4, which is characterized in that be added to first extraction
It is (1~5) to take the mass ratio of the extractant in rectifying column and the raw material:1；It is added in second extractive distillation column
The mass ratio of extractant and the raw material is (1~5):1.
6. the method for Separation of Benzene according to claim 3, hexamethylene, cyclohexene, which is characterized in that the first extraction essence
1~2MPa of pressure of tower is evaporated, column bottom temperature is 140~180 DEG C, and tower top temperature is 80~110 DEG C；Second extractive distillation column
Pressure for 1~2MPa, column bottom temperature is 240~280 DEG C, and tower top temperature is 80~110 DEG C；The pressure of the rectifying column is 1
~2MPa, column bottom temperature are 240~280 DEG C, and tower top temperature is 80~110 DEG C.
7. the method for Separation of Benzene according to claim 6, hexamethylene, cyclohexene, which is characterized in that the first extraction essence
The reflux ratio for evaporating tower is 0.1~2；The reflux ratio of second extractive distillation column is 1~10；The reflux ratio of the rectifying column is 1
~10.
8. the method for Separation of Benzene according to claim 6, hexamethylene, cyclohexene, which is characterized in that the first extraction essence
The reflux ratio for evaporating tower is 0.5~1.5；The reflux ratio of second extractive distillation column is 2~6；The reflux ratio of the rectifying column is 4
~8.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711480168.7A CN108046974B (en) | 2017-12-29 | 2017-12-29 | System and method for separating benzene, cyclohexane and cyclohexene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711480168.7A CN108046974B (en) | 2017-12-29 | 2017-12-29 | System and method for separating benzene, cyclohexane and cyclohexene |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109053350A (en) * | 2018-09-21 | 2018-12-21 | 成都科特瑞兴科技有限公司 | A kind of cyclohexyl benzene production system and the technique using the system production cyclohexyl benzene |
| CN112661593A (en) * | 2021-02-05 | 2021-04-16 | 郑州轻工业大学 | Method for separating benzene, cyclohexene and cyclohexane by extractive distillation of mixed solvent containing ionic liquid |
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| CN102134177A (en) * | 2011-02-28 | 2011-07-27 | 河北民海化工有限公司 | Method for separating cyclohexane and cyclohexene by extraction and rectification |
| CN102690161A (en) * | 2012-05-31 | 2012-09-26 | 中国天辰工程有限公司 | Separating method for benzene-cyclohexane-cyclohexene |
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| JPS51127043A (en) * | 1975-04-24 | 1976-11-05 | Toray Ind Inc | Process for purification of cyclohexene |
| JPS58172323A (en) * | 1982-04-02 | 1983-10-11 | Asahi Chem Ind Co Ltd | Separation of monocyclic monoolefin |
| JPH01135730A (en) * | 1987-11-24 | 1989-05-29 | Asahi Chem Ind Co Ltd | Method for separating cyclohexene by mixed solvent |
| CN102134177A (en) * | 2011-02-28 | 2011-07-27 | 河北民海化工有限公司 | Method for separating cyclohexane and cyclohexene by extraction and rectification |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109053350A (en) * | 2018-09-21 | 2018-12-21 | 成都科特瑞兴科技有限公司 | A kind of cyclohexyl benzene production system and the technique using the system production cyclohexyl benzene |
| CN109053350B (en) * | 2018-09-21 | 2023-11-03 | 成都科特瑞兴科技有限公司 | Cyclohexylbenzene production system and process for producing cyclohexylbenzene by using same |
| CN112661593A (en) * | 2021-02-05 | 2021-04-16 | 郑州轻工业大学 | Method for separating benzene, cyclohexene and cyclohexane by extractive distillation of mixed solvent containing ionic liquid |
| CN112661593B (en) * | 2021-02-05 | 2023-07-18 | 郑州轻工业大学 | Method for separating benzene, cyclohexene and cyclohexane by extracting and rectifying mixed solvent containing ionic liquid |
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| CN108046974B (en) | 2020-10-30 |
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