CN105367448B - A kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN separation method and system - Google Patents
A kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN separation method and system Download PDFInfo
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- CN105367448B CN105367448B CN201510884571.0A CN201510884571A CN105367448B CN 105367448 B CN105367448 B CN 105367448B CN 201510884571 A CN201510884571 A CN 201510884571A CN 105367448 B CN105367448 B CN 105367448B
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- 2m3bn
- 2m2bn
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/32—Separation; Purification; Stabilisation; Use of additives
- C07C253/34—Separation; Purification
Abstract
A kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN separation method and system, the present invention proposes meeting by-product 2M2BN during 2M3BN isomerization generation 3PN, and 2M2BN can be accumulated constantly in systems, suppress the progress of isomerization reaction, increase 2M2BN and 2M3BN relative volatility by extractant of the present invention, 2M2BN and 2M3BN separation and recycling for extractant are completed in the same rectifying column with dividing plate, greatly reduce equipment cost and operation difficulty, it is possible to obtain 2M2BN the and 2M3BN products of high-purity.
Description
Technical field
The invention belongs to technical field of chemical separation, more particularly to a kind of 2M3BN isomerization production 3PN byproduct in process things
2M2BN separation method and system.
Background technology
3 pentene nitrile (3PN) is the intermediate for preparing adiponitrile, can continue hydrocyanation for adiponitrile, and adiponitrile is Buddhist nun
Imperial 66 intermediates, belong to important chemical products.2- methyl -3- butene nitriles (2M3BN) isomerization produces 3 pentene nitrile (3PN) mistake
Meeting by-product 2- methyl-2-butenes nitrile (2M2BN) in journey, and 2M2BN meetings accumulation constantly in reaction system, cause reaction conversion ratio
With selective reduction, it is therefore desirable to which by 2M2BN, continuous separation is produced from reaction system.However, 2M2BN and 2M3BN normal pressure
Boiling-point difference is too small, less than 5 DEG C, needs high tower diameter and big reflux ratio with conventional distillation method, causes operating cost and operating cost
It is higher.
A kind of methods of alkene nitrile mixed liquor Direct Isomerization synthesis 3 pentene nitrile of patent CN201410052580.9 are proposed
Zero-valent nickel catalyst, phosphorus-containing ligand and lewis acid, 2- methyl -3- butylene are added in 2- methyl -3- butene nitriles and 3 pentene nitrile
Nitrile can be isomerized to 3 pentene nitrile, and 2M3BN selectivity of the conversion ratio more than 95%, 3PN, which is more than in 95%, patent, not to be carried
2M2BN accessory substances can be produced by going out isomerization reaction.
The method that a kind of alkene nitrile mixed liquor Direct Isomerizations of patent CN201410052751.8 synthesize 2- methyl-2-butene nitriles
Propose to add calcic inorganic base in 2- methyl -3- butene nitriles and 3 pentene nitrile can occur isomerization reaction generation 2M2BN, should
Patent only shows that inorganic base can make 2M3BN isomerization generate 3PN reactions and occur towards side reaction 2M2BN directions, does not refer to 2M3BN
With 2M2BN separation method.
The content of the invention
The present invention, which is proposed, uses extractant, increases 2M2BN and 2M3BN boiling-point difference, recycles the rectifying of specific structure
Tower carries out continuous rectification, so as to realize 2M2BN and 2M3BN separation, the concrete technical scheme of use is as follows：
A kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN separation method, comprises the following steps：
Step 1：Dividing plate is set in rectifying column, tower body inside upper part is divided into two regions in left and right, tower body bottom is not divide
Every public domain, 2M2BN and 2M3BN mixed materials feed from rectifying column left field middle and lower part, and extractant is left from rectifying column
Side region its top feed；
Step 2：2M2BN is obtained at the top of rectifying column left field, 2M3BN enters tower reactor public domain with extractant；
Step 3：Circulating-heating is carried out in public domain, into the right side area of rectifying column, by 2M3BN and extractant point
From acquisition 2M3BN at the top of rectifying column right side area, extractant returns to tower reactor public domain and recycled.
Rectifying tower pressure on top surface is 10-50kPaA, and column bottom temperature is 100-120 DEG C, rectifying column diameter 300mm, and tower height is not
Less than 6000mm, the shared height in the public domain after dividing plate is set to be no more than the 20% of rectifying column tower height in rectifying column.
The extractant is one kind in trimethyl phosphate or dimethyl sulfoxide (DMSO).Poor solubility of the extractant to two kinds of components
Not larger, the dissolubility to 2M3BN is much larger than 2M2BN dissolubility, and extractant is poorer than 2M2BN and 2M3BN volatility,
2M2BN can be separated from isomerization reaction system by extraction rectifying method.
In 2M2BN the and 2M3BN mixtures, 2M2BN and 2M3BN are according to mass ratio 1:1 proportioning.
A kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN piece-rate system, including tower bottom reboiler, tower top
2M3BN coolers, tower top 2M2BN coolers, rectifying column, head tank, feed pump, head tank are connected by feed pump and rectifying column
Connect, rectifier bottoms, which are set, sets dividing plate in tower bottom reboiler, rectifying column, tower body inside upper part is divided into two regions in left and right,
Tower body bottom is the public domain not separated, and left field tower top sets tower top 2M2BN coolers, and right side area tower top sets tower
Push up and extractant feed mouthful is set at the top of 2M3BN coolers, rectifying column left field.
The shared height in the public domain after dividing plate is set to be no more than the 20% of rectifying column tower height in the rectifying column.Rectifying column
Diameter 300mm, tower height is not less than 6000mm.Head tank is connected by feed pump with rectifying column left field middle and lower part.
What 2M3BN was represented in the present invention is 2- methyl -3- butene nitriles, and what 3PN was represented is 3 pentene nitrile, what 2M2BN was represented
It is 2- methyl-2-butene nitriles.The present invention sets the rectifying column of dividing plate using centre, and region in tower is divided into left field by dividing plate,
Right side area and bottom public domain.Left field realizes 2M2BN extracting rectifying, and right side area realizes 2M3BN rectifying,
Bottom public domain is stripping region, completes the recovery of extractant.2M2BN and the 2M3BN left side central portion from tower enter, extractant
Added from left side top of tower, because extractant is much larger than 2M2BN to 2M3BN dissolubility, left side top can obtain pure
2M2BN, 2M3BN enter tower reactor public domain with extractant, in public domain by circulating-heating, real into the right side area of tower
Separation of the existing 2M3BN with trimethyl phosphate.
The beneficial effects of the invention are as follows：The present invention proposes meeting by-product 2M2BN during 2M3BN isomerization generation 3PN, and
2M2BN can be accumulated constantly in systems, suppress isomerization reaction progress, by extractant of the present invention increase 2M2BN and
2M3BN relative volatility, 2M2BN and 2M3BN separation and extractant is completed in the same rectifying column with dividing plate
Recycle, greatly reduce equipment cost and operation difficulty, it is possible to obtain 2M2BN the and 2M3BN products of high-purity.
Brief description of the drawings
Fig. 1 is generation accessory substance 2M2BN accumulation schematic diagrames during 2M3BN isomerization production 3PN
Fig. 2 is that 2M3BN isomerization of the present invention produces 3PN byproduct in process thing 2M2BN piece-rate system structure charts
Marginal data：1st, tower bottom reboiler, 2, tower top 2M3BN coolers, 3, tower top 2M2BN coolers, 4, rectifying column, 5,
Head tank, 6, feed pump, 7, dividing plate, 8, left field, 9, right side area, 10, public domain, 11, extractant feed mouthful
A, 2M3BN, B, 2M2BN, C, 3PN, D, catalyst, E, extractant, F, left field top products, G, right side area
Top products
Embodiment
In order that the technical means, the inventive features, the objects and the advantages of the present invention are easy to understand, below it is right
The embodiment of the present invention is described further, but does not limit protection scope of the present invention, it is necessary to which explanation, is not being rushed
In the case of prominent, the feature in embodiment and embodiment in the invention can be mutually combined.
As shown in figure 1,2M3BNA and catalyst D are continuously added in diameter 600mm, height 800mm carbon steel reactor,
Catalyst D inlet amounies 1kg/h, 2M3BNA inlet amount 100kg/h, opens stirring, reaction time about 2h.Taken in exit analysis
Sample, finds there is unreacted 2M3BN, accessory substance 2M2BNB and reaction product 3PNC, 2M2BNB content about 5w.t% in product, not
2M3BN contents about 30w.t%, 3PNC the content 65w.t% of reaction, it is possible thereby to illustrate there is 2M2BNB generation in reaction.
Reaction as shown in Figure 1 is separately carried out, 2M3BNA is added in diameter 600mm, height 800mm carbon steel reactor,
2M3BNA addition 200kg are controlled, while adding catalyst D, catalyst D addition 2kg are controlled, stirring is opened, measurement is different
Under reaction time, 2M2BN contents, 2M3BN contents, 3PN contents, measurement data is as shown in table 1.
The measurement data list of table 1
| Reaction time (h) | 2M2BN contents (w.t%) | 2M3BN contents (w.t%) | 2M2BN contents (w.t%) |
| 3 | 15 | 21 | 64 |
| 4 | 18 | 20 | 62 |
| 5 | 21 | 19 | 60 |
By table 1 it can be found that with the extension in reaction time, 2M2BN content is being continuously increased in reaction system, and it is secondary
Product 2M2BN can suppress 2M3BN isomerization reactions, and 3PN can inversely be converted into 2M2BN as time went on.
Embodiment 1：
A kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN piece-rate system, including tower bottom reboiler 1, tower
Push up 2M3BN coolers 2, tower top 2M2BN coolers 3, rectifying column 4, head tank 5, feed pump 6, head tank 5 by feed pump 6 with
Rectifying column 4 is connected, and the bottom of rectifying column 4, which is set, sets dividing plate 7 in tower bottom reboiler 1, rectifying column 4, tower body inside upper part is divided into
Left field 8 and right side area 9, tower body bottom are the public domain 10 not separated, and the tower top of left field 8 sets tower top 2M2BN
Cooler 3, the tower top of right side area 9 sets tower top 2M3BN coolers 2, and the top of 4 left field of rectifying column 8 sets extractant feed
Mouth 11.
The diameter 300mm of rectifying column 4, tower height 6000mm, interior setting dividing plate 7, by tower body inside upper part be divided into left field 8 with
Right side area 9, tower body bottom is the public domain 10 not separated, and the shared height in 4 bottom public domain of rectifying column 10 is total tower height
20%, by 2M2BN and 2M3BN according to mass ratio 1：1 matches in head tank 5, and it is left to send into the rectifying column 4 by feed pump 6
The middle and lower part of side region 8, extractant E trimethyl phosphates control rectifying amount 200kg/h by its top feed of 4 left field of rectifying column 8,
100 DEG C of control tower bottom vapo(u)rizing temperature, tower top pressure 10kPaA, using continuous distillation method, 2M2BN and 2M3BN mixed materials from
Middle and lower part is added on the left of tower, and extractant E trimethyl phosphates are added from the top of tower left field 8, control extractant addition
300kg/h, because extractant E trimethyl phosphates are much larger than 2M2BN to 2M3BN dissolubility, the top of left field 8 can obtain pure
2M2BN, 2M3BN with extractant E trimethyl phosphates enter tower reactor public domain 10, in public domain 10 by tower bottom reboiler 1
Circulating-heating, into the right side area 9 of rectifying column, realizes separation of the 2M3BN with trimethyl phosphate.Respectively to tower top left field
8 and the top products of right side area 9 analyzed, it is found that 2M2BN contents are more than 99.99w.t% in left field top products F,
2M3BN contents are more than 99.99wt% in right side area top products G, show to be successfully realized in the rectifying column 4 2M2BN and
2M3BN separation, and extractant E trimethyl phosphates will not be entrained in product 2M2BN and 2M3BN.Extractant E phosphorus in tower reactor
Sour trimethyl can feed back to extractant feed mouthful 11, be recycled.
Embodiment 2：
A kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN piece-rate system, including tower bottom reboiler 1, tower
Push up 2M3BN coolers 2, tower top 2M2BN coolers 3, rectifying column 4, head tank 5, feed pump 6, head tank 5 by feed pump 6 with
Rectifying column 4 is connected, and the bottom of rectifying column 4, which is set, sets dividing plate 7 in tower bottom reboiler 1, rectifying column 4, tower body inside upper part is divided into
Left field 8 and right side area 9, tower body bottom are the public domain 10 not separated, and the tower top of left field 8 sets tower top 2M2BN
Cooler 3, the tower top of right side area 9 sets tower top 2M3BN coolers 2, and the top of 4 left field of rectifying column 8 sets extractant feed
Mouth 11.
The diameter 300mm of rectifying column 4, tower height 7000mm, interior setting dividing plate 7, by tower body inside upper part be divided into left field 8 with
Right side area 9, tower body bottom is the public domain 10 not separated, and the shared height in 4 bottom public domain of rectifying column 10 is no more than total
The 20% of tower height, by 2M2BN and 2M3BN according to mass ratio 1：1 is matched in head tank 5, and the rectifying column is sent into by feed pump 6
The middle and lower part of 4 left field 8, extractant E dimethyl sulfoxide (DMSO)s are by its top feed of 4 left field of rectifying column 8, control rectifying amount 200kg/
H, 120 DEG C of control tower bottom vapo(u)rizing temperature, tower top pressure 50kPaA, using continuous distillation method, 2M2BN and 2M3BN mixed materials
Middle and lower part is added on the left of from tower, and extractant E dimethyl sulfoxide (DMSO)s are added from the top of tower left field 8, control extractant addition
300kg/h, because extractant E dimethyl sulfoxide (DMSO)s are much larger than 2M2BN to 2M3BN dissolubility, the top of left field 8 can obtain pure
2M2BN, 2M3BN with extractant E dimethyl sulfoxide (DMSO)s enter tower reactor public domain 10, in public domain 10 by tower bottom reboiler 1
Circulating-heating, into the right side area 9 of rectifying column, realizes separation of the 2M3BN with dimethyl sulfoxide (DMSO).Respectively to tower top left field
8 and the top products of right side area 9 analyzed, it is found that 2M2BN contents are more than 99.99w.t% in left field top products F,
2M3BN contents are more than 99.99wt% in right side area top products G, show to be successfully realized in the rectifying column 4 2M2BN and
2M3BN separation, and extractant E dimethyl sulfoxide (DMSO)s will not be entrained in product 2M2BN and 2M3BN.Extractant E bis- in tower reactor
Methyl sulfoxide can feed back to extractant feed mouthful 11, be recycled.
Embodiment 3：
A kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN piece-rate system, including tower bottom reboiler 1, tower
Push up 2M3BN coolers 2, tower top 2M2BN coolers 3, rectifying column 4, head tank 5, feed pump 6, head tank 5 by feed pump 6 with
Rectifying column 4 is connected, and the bottom of rectifying column 4, which is set, sets dividing plate 7 in tower bottom reboiler 1, rectifying column 4, tower body inside upper part is divided into
Left field 8 and right side area 9, tower body bottom are the public domain 10 not separated, and the tower top of left field 8 sets tower top 2M2BN
Cooler 3, the tower top of right side area 9 sets tower top 2M3BN coolers 2, and the top of 4 left field of rectifying column 8 sets extractant feed
Mouth 11.
The diameter 300mm of rectifying column 4, tower height 6500mm, interior setting dividing plate 7, by tower body inside upper part be divided into left field 8 with
Right side area 9, tower body bottom is the public domain 10 not separated, and the shared height in 4 bottom public domain of rectifying column 10 is no more than total
The 20% of tower height, by 2M2BN and 2M3BN according to mass ratio 1：1 is matched in head tank 5, and the rectifying column is sent into by feed pump 6
The middle and lower part of 4 left field 8, extractant E trimethyl phosphates are by its top feed of 4 left field of rectifying column 8, control rectifying amount 200kg/
H, 110 DEG C of control tower bottom vapo(u)rizing temperature, tower top pressure is in 30kPaA scopes, using continuous distillation method, and 2M2BN and 2M3BN are mixed
Compound material is added from middle and lower part on the left of tower, and extractant E trimethyl phosphates are added from the top of tower left field 8, and control extractant adds
Enter amount 300kg/h, because extractant E trimethyl phosphates are much larger than 2M2BN to 2M3BN dissolubility, the top of left field 8 can be obtained
Pure 2M2BN is obtained, 2M3BN enters tower reactor public domain 10 with extractant E trimethyl phosphates, boiled again by bottom of towe in public domain 10
The circulating-heating of device 1, into the right side area 9 of rectifying column, realizes separation of the 2M3BN with trimethyl phosphate.Respectively on the left of tower top
Region 8 and the top products of right side area 9 are analyzed, it is found that 2M2BN contents exceed in left field top products F
2M3BN contents show that success is real in the rectifying column 4 more than 99.99wt% in 99.99w.t%, right side area top products G
Show 2M2BN and 2M3BN separation, and extractant E trimethyl phosphates will not be entrained in product 2M2BN and 2M3BN.In tower reactor
Extractant E trimethyl phosphates can feed back to extractant feed mouthfuls 11, recycled.
Separation method of the present invention and system are described by specific embodiment.People in the art
Member can use for reference present disclosure and suitably change the links such as rectifying tower structure to realize corresponding other purposes, and its correlation changes
All without departing from present disclosure, all any modifications within the spirit and principle of the invention, made, equally replace
Change, improve, should be included within the protection domain of the invention.
Claims (2)
1. a kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN separation method, it is characterised in that the extraction used
Agent is one kind in trimethyl phosphate or dimethyl sulfoxide (DMSO)；
This method comprises the following steps：
Step 1：Dividing plate is set in rectifying column, tower body inside upper part is divided into two regions in left and right, tower body bottom does not separate
Public domain, 2M2BN and 2M3BN mixed materials are fed from rectifying column left field, and extractant is at the top of rectifying column left field
Charging；
Step 2：2M2BN is obtained at the top of rectifying column left field, 2M3BN enters tower reactor public domain with extractant；
Step 3：2M3BN enters the right side area of rectifying column with extractant from public domain, and 2M3BN is separated with extractant, essence
Evaporate and 2M3BN is obtained at the top of tower right side area；
The rectifying tower pressure on top surface is 10-50kPaA；Rectifying column column bottom temperature is 100-120 DEG C；Dividing plate is set in rectifying column
The shared height in public domain afterwards is no more than the 20% of rectifying column tower height；Rectifying column diameter 300mm, tower height is not less than 6000mm；
In 2M2BN the and 2M3BN mixtures, 2M2BN and 2M3BN are according to mass ratio 1:1 proportioning.
2. a kind of 2M3BN isomerization production 3PN byproduct in process things 2M2BN piece-rate system, it is characterised in that set in rectifying column
Dividing plate is put, tower body inside upper part is divided into two regions in left and right, tower body bottom is the public domain not separated, left field tower top
Tower top 2M2BN coolers are set, and right side area tower top, which is set, sets extraction at the top of tower top 2M3BN coolers, rectifying column left field
Take and set the shared height in the public domain after dividing plate to be no more than the 20% of rectifying column tower height, institute in agent charging aperture, the rectifying column
Rectifying column diameter 300mm is stated, tower height is not less than 6000mm.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1914165A (en) * | 2004-01-29 | 2007-02-14 | 巴斯福股份公司 | Homogeneous isomerization of cis-2-pentene nitrile to form 3-pentene nitrile |
| CN1914164A (en) * | 2004-01-29 | 2007-02-14 | 巴斯福股份公司 | Isomerization of cis-2-pentenenitrile to form 3-pentenenitrile in a reactive distillation |
| CN104254520A (en) * | 2012-04-27 | 2014-12-31 | 巴斯夫欧洲公司 | Process for isomerizing cis-2-pentenenitrile to 3-pentenenitriles |
| CN205501166U (en) * | 2015-12-04 | 2016-08-24 | 中国天辰工程有限公司 | Piece -rate system of 2 - methyl - 3 - crotononitrile isomerization production 3 - allyl acetonitrile in -process accessory substance 2 - methyl - 2 - crotononitrile |
-
2015
- 2015-12-04 CN CN201510884571.0A patent/CN105367448B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1914165A (en) * | 2004-01-29 | 2007-02-14 | 巴斯福股份公司 | Homogeneous isomerization of cis-2-pentene nitrile to form 3-pentene nitrile |
| CN1914164A (en) * | 2004-01-29 | 2007-02-14 | 巴斯福股份公司 | Isomerization of cis-2-pentenenitrile to form 3-pentenenitrile in a reactive distillation |
| CN104254520A (en) * | 2012-04-27 | 2014-12-31 | 巴斯夫欧洲公司 | Process for isomerizing cis-2-pentenenitrile to 3-pentenenitriles |
| CN205501166U (en) * | 2015-12-04 | 2016-08-24 | 中国天辰工程有限公司 | Piece -rate system of 2 - methyl - 3 - crotononitrile isomerization production 3 - allyl acetonitrile in -process accessory substance 2 - methyl - 2 - crotononitrile |
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