CN106478455A - The removal methods of micro hydrocyanic acid in acetonitrile refining system - Google Patents
The removal methods of micro hydrocyanic acid in acetonitrile refining system Download PDFInfo
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- CN106478455A CN106478455A CN201510532801.7A CN201510532801A CN106478455A CN 106478455 A CN106478455 A CN 106478455A CN 201510532801 A CN201510532801 A CN 201510532801A CN 106478455 A CN106478455 A CN 106478455A
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Abstract
The present invention relates in a kind of acetonitrile refining micro hydrocyanic acid removal methods, described main method includes：In dehydrogenation cyanic acid tower, chemical treatment, decompression, the group technology flow process of pressurization azeotropic distillation, by adding alkali compoundss to obtain acetonitrile of high purity using in vacuum distillation tower.
Description
Technical field
The present invention relates to micro hydrocyanic acid removal methods in a kind of high-purity acetonitrile refining.
Background technology
In process for production of acrylonitrile, acetonitrile, hydrocyanic acid (HCN) as by-product recovery, and
The impurity such as aldehyde, ketone and a small amount of hydrocyanic acid are extracted to aqueous acetonitrile in acrylonitrile extraction process
In liquid, through acetonitrile desorbing or air stripping in crude acetonitrile.Generally using by decyanation tower, chemistry
Reason, decompression, the group technology of pressurization azeotropic distillation, are continuously reclaimed to acetonitrile, can be effective
The impurity such as water and acrylic aldehyde, propionitrile, acetone, propenyl in ground removing acetonitrile.
However, due to the cyanalcohol condensation substance unstable with aldehyde, ketone condensation generation of HCN in thing system,
And progressively decomposite free HCN in distillation process, so that the separation process of HCN is complicated
Change so that combinations thereof technique becomes a kind of distillation process with decomposition reaction, so to micro-
The separation of amount HCN can not be completed it is necessary to examine simultaneously by conventional, single distillation operation
Consider the impact of physical factor and chemical factor, the separation of micro HCN is placed in whole process and examines
Consider, be finally reached the requirement of microseparation index.
EP055920 discloses a kind of continuous technique reclaiming acetonitrile.This technique adopts rectification to remove
The Light ends such as hydrocyanic acid, plus alkali and plus formaldehyde chemical treatment remove further hydrocyanic acid, decompression essence
Evaporate the method with compression rectification combined dehydration, improve the refined recovery rate of acetonitrile, can get relatively
Highly purified acetonitrile product.But the process adds plus formaldehyde chemical treatment step, complex operation.
CN1102575C discloses a kind of continuous technique reclaiming acetonitrile.By subtracting in traditional
The rectifying section of pressure rectifying column and compression rectification tower sets up an alkali metal hydroxide or alkaline-earth metal
The charging aperture of hydroxide, alkali compoundss are added in local, the bar being heated in alkalescence using cyanalcohol
Free HCN can be decomposited under part, and the HCN decompositing easily is generated with alkaline metal cpds
Stable compound, thus the characteristic removing by rectification, makes to decompose out in distillation process
HCN can successfully discharge from tower bottom of rectifying tower, reaches the purpose of micro HCN in removing acetonitrile.
But the charging aperture of this technique alkali metal hydroxide or alkaline earth metal hydroxide limitation is distributed with
Property it is necessary to opening and can not cover all enforcement a little is increased on tower.
Content of the invention
It is an object of the invention to provide micro hydrocyanic acid during a kind of improved high-purity acetonitrile refining
Removal methods, to overcome hydrocyanic acid content in acetonitrile product present in prior art higher or second
The defect of nitrile subtractive process complex operation.
For achieving the above object, the present invention provides micro hydrocyanic acid in a kind of high-purity acetonitrile refining to take off
Except method, to connect from containing acetonitrile, water, the crude acetonitrile of light component, HCN and weight Organic substance
Continuous recovery high-purity acetonitrile, the method comprises the following steps：
A) described raw material crude acetonitrile is delivered in the first knockout tower, by Light ends and major part
HCN is discharged by the tower top of described first knockout tower, by part water and weight Organic substance by described first
The tower reactor of knockout tower is discharged, and takes out from the stripping section bottom side line gas phase of described first knockout tower
Go out containing water-acetonitrile；
B) it is delivered to described chemical treatment kettle containing water-acetonitrile and carries out plus alkali chemical treatment, to remove
Free HCN, thus obtain reactant liquor acetonitrile；
C) described reactant liquor acetonitrile is delivered to the second knockout tower of decompression, in this second knockout tower
Any plate position of rectifying section at or overhead reflux liquid porch add alkali liquor, this second separate
The tower reactor removing weight Organic substance of tower, and second separate tower top and steam and be stripped of most of water from this
Acetonitrile；And
D) the described acetonitrile being stripped of most of water is delivered to the 3rd knockout tower of pressurization, makes this
Return the second knockout tower after the aqueous acetonitrile material condensation that the tower top of the 3rd knockout tower steams to enter
Material, and extract described high-purity acetonitrile out from the stripping pars infrasegmentalis gas phase of the 3rd knockout tower.
Preferably, in described first knockout tower, tower top pressure is 0.10～0.125MPa, enters
Material temperature degree is 30～80 DEG C, and tower top drop temperature is 35～60 DEG C, stripping section lateral line withdrawal function temperature
For 85～100 DEG C, bottom temperature is 105～120 DEG C.
Preferably, in described second knockout tower, tower top pressure is 0.013～0.040Mpa, enters
Material temperature degree is 30～50 DEG C, and tower top temperature is 30～50 DEG C, and bottom temperature is 50～75 DEG C.
Preferably, described alkali liquor is the water-soluble of alkali metal hydroxide or alkaline earth metal hydroxide
Liquid.
Preferably, described alkali metal hydroxide or alkaline earth metal hydroxide be sodium hydroxide,
Potassium hydroxide or calcium hydroxide.
Preferably, described alkali metal hydroxide or alkaline earth metal hydroxide are sodium hydroxide.
Preferably, the concentration of described alkali liquor is 1～40wt%.
Preferably, the concentration of described alkali liquor is 10～20wt%.
Preferably, the mass flow of described alkali liquor is to add the described reaction of described second knockout tower
The 1～10% of the mass flow of liquid acetonitrile.
Preferably, the mass flow of described alkali liquor is to add the described reaction of described second knockout tower
The 1～5% of the mass flow of liquid acetonitrile.
Preferably, the mass flow of described alkali liquor is to add the described reaction of described second knockout tower
The 2～3% of the mass flow of liquid acetonitrile.
Preferably, the alkali liquor charging aperture for adding described alkali liquor is located at described second knockout tower
At the plate position more than plate position that charging aperture is located.
Preferably, described alkali liquor charging aperture be located at described second knockout tower tower top to tower top down
To any plate position of charging aperture 10% column plate.
Preferably, add described alkali liquor through described overhead reflux liquid entrance.
Preferably, in described 3rd knockout tower, tower top pressure is 0.1～0.5MPa, charging
Temperature be 30～90 DEG C, tower top temperature be 90～140 DEG C, stripping section lateral line withdrawal function temperature be 100～
135 DEG C, bottom temperature is 110～145 DEG C.
The effect of the present invention
According to the present invention, an alkali metal is set up by the rectifying section in the second traditional knockout tower
Hydroxide or the charging aperture of alkaline earth metal hydroxide, or utilize overhead reflux liquid entrance, office
Portion adds alkali compoundss, can decomposite free HCN using cyanalcohol under conditions of alkalescence heating,
And the compound that HCN is easy and alkaline metal cpds generation is stable decompositing, thus passing through
The characteristic that rectification removes, enables the HCN decomposing out in distillation process successfully from rectifying tower
Kettle is discharged, and reaches the purpose of micro HCN in removing acetonitrile.Do not add additionally, due to the present invention
Any equipment and the chemical treating process increasing complexity, especially with overhead reflux liquid entrance more
Can avoid increasing opening on tower, therefore easy and simple to handle, achieve preferable effect.
Brief description
Fig. 1 is micro hydrocyanic acid removal methods schematic diagram in the high-purity acetonitrile refining of the present invention.
In Fig. 1,1 is the first knockout tower, and 2 is the first knockout tower condenser, and 3 is chemical reaction
Kettle, 4 is alkali liquor surge tank, and 5 is lye pump, and 6 is the second knockout tower, and 7 is the second knockout tower
Condenser, 8 is the second knockout tower reflux pump, and 9 is the 3rd knockout tower, and 10 is that the 3rd knockout tower is cold
Condenser.
Specific embodiment
As shown in figure 1, raw material crude acetonitrile 11 pass through feed line 12 from be positioned first separate
Material inlet 13 in the middle part of tower enters the first knockout tower.Raw material crude acetonitrile 11 can comprise part
The acetonitrile of purification, can come from any suitable source, for example, from acrylonitrile installation acetonitrile
Desorbing tower top.By weight percentage, the composition of raw material crude acetonitrile can include 20～80% second
Nitrile, 1～4% HCN, 0.1～0.3% acrylonitrile and 20～79% water.
After the gaseous stream 14 of the first knockout tower 1 tower top condenses through the first knockout tower condenser 2,
Lime set 15 all flows back, and the on-condensible gas such as most of hydrocyanic acid and Light ends 16 discharge system takes off
Remove." light component " described herein is the other impurity in addition to hydrocyanic acid, such as acrylonitrile,
Azoles etc..Tower reactor exclusive segment water and heavy component 17 by the first knockout tower.It is stripped of Light ends
Extract out from the stripping section bottom side line gas phase of the first knockout tower 1 containing water-acetonitrile 18, defeated after condensation
Deliver to chemical treatment kettle 3.Preferably, the tower top pressure of the first knockout tower 1 is 0.10～0.125
MPa, feeding temperature is 30～80 DEG C, and tower top drop temperature is 35～60 DEG C, stripping section side line
Extract temperature out and be 85～100 DEG C, bottom temperature is 105～120 DEG C.
In chemical reaction kettle 3, sodium hydroxide solution 19 is added to carry out chemical treatment, to remove
The impurity such as free hydrocyanic acid and a small amount of acrylonitrile, chemically treated after reactant liquor acetonitrile 20 enter
Second knockout tower 6.
The rectifying section of the second knockout tower 6 is configured with alkali liquor charging aperture 23, and lye pump 5 and alkali liquor enter
It is configured with the first pipeline 24, the first pipeline 24 is arranged to buffer alkali liquor between material mouth 23
Alkali liquor 22 in tank 4 is transported to the rectifying section of the second knockout tower 6 via lye pump 5；Second point
It is configured with second pipe 26 from the outlet of tower reflux pump 8；Second pipe 26 outlet is configured with flow
Controller 28, flow controller 28 is configurable for controlling the capacity of returns of the second knockout tower 6；
Second pipe 26 is arranged to the condensation material 27 of the second knockout tower condenser 7 through backflow
Pump 8 is delivered to flow controller 28 and the 3rd knockout tower 9；The rectifying section top of the second knockout tower 6
Portion is configured with backflow entrance 25, is configured between flow controller 28 and backflow entrance 25
3rd pipeline 29, the 3rd pipeline 29 is arranged to for backflow material to be delivered to backflow entrance
25；It is configured with junction point 30 on 3rd pipeline 29；Configure between lye pump 5 and junction point 30
There is the 4th pipeline 31, the 4th pipeline 31 is arranged to convey alkali liquor entrance backflow entrance 25.
Alkali liquor in alkali liquor surge tank 4 is preferably alkali metal hydroxide or alkaline-earth metal hydroxide
The aqueous solution of thing.The concentration of alkali liquor is preferably 1～60wt%, more preferably 1～40wt%, enters one
Step is preferably 10～20wt%.Described alkali metal hydroxide or alkaline earth metal hydroxide are hydrogen-oxygen
Change sodium, potassium hydroxide or calcium hydroxide, more preferably sodium hydroxide.The addition of alkali liquor is preferred
For adding the 1～10% of the mass flow of the reactant liquor acetonitrile 20 of the second knockout tower, more preferably
1～5%, still more preferably 2～3%.
The chemically treated reactant liquor acetonitrile 20 removing the impurity such as free hydrocyanic acid separates from second
Tower 6 middle part charging aperture 21 enters the second knockout tower 6.Alkali liquor 22 is from alkali liquor surge tank 4 through alkali liquor
The alkali liquor charging aperture 23 that pump 5 is delivered to above the charging aperture at the second knockout tower 6 middle part enters second point
From tower.The plate position that alkali liquor charging aperture 23 is located is not specifically limited, as long as it is in charging aperture 21
The top of place plate position, but preferably, alkali liquor charging aperture is located at the tower top of the second knockout tower
At to tower top down to any plate position of charging aperture 10% column plate.Or it is preferable that by alkali liquor
22 are delivered to the 3rd pipeline 29, enter the second knockout tower 6 via backflow entrance 25.
In the second knockout tower 6, the impurity 33 comprising heavy component and water etc. is excluded from tower reactor.De-
The acetonitrile 32 removing most of water is distillated to the second knockout tower condenser by the second knockout tower 6 top
7, after condensed cooling, a part of material passes back into second through the second knockout tower reflux pump 8 and separates
Column overhead backflow entrance 25, rest materials enter the 3rd knockout tower 9.
Preferably, in the second knockout tower 6, tower top pressure is 0.013～0.040Mpa, enters
Material temperature degree is 30～50 DEG C, and tower top temperature is 30～50 DEG C, and bottom temperature is 50～75 DEG C.
The acetonitrile material 34 of the water content of tower top of the 3rd knockout tower 9 is through the 3rd knockout tower condenser
After 10 condensation coolings, partial material is back to refluxing opening 35, and rest materials 36 return second point
From tower 6 charging aperture 21 or the first knockout tower charging aperture 13；Tower reactor contains the acetonitrile material of heavy constituent
38 return the second knockout tower 6 charging apertures 21；Through the second knockout tower 6, the subtracting of the 3rd knockout tower 9
After pressure, pressurization combination dehydration, from the gas phase side of the stripping pars infrasegmentalis being arranged on the 3rd knockout tower 9
Line outlet port 37, obtains high-purity finished product acetonitrile 39.
Preferably, in the 3rd knockout tower 9, tower top pressure is 0.1～0.5MPa, enters material temperature
Spend for 30～90 DEG C, tower top temperature is 90～140 DEG C, stripping section lateral line withdrawal function temperature is 100～135
DEG C, bottom temperature is 110～145 DEG C.
Embodiment
Below by embodiment, the invention will be further elaborated, but the invention is not restricted to following
Embodiment.
【Embodiment 1】
On the basis of comparative example 1, increase at vacuum distillation tower charging aperture up the 3rd block of plate
Alkali liquor charging aperture, is that 10%NaOH is molten by 1% addition weight percent concentration of feed weight
Liquid, excludes the impurity such as water and propenyl, propionitrile, Cyanogran. from vacuum distillation tower tower reactor.Thick second
With weight in nitrile, containing acetonitrile 50%, hydrocyanic acid 1.5%.Essence through above flow process
System, in finished product acetonitrile, hydrocyanic acid is 10ppm.
【Embodiment 2】
On the basis of comparative example 1, increase at vacuum distillation tower charging aperture up the 3rd block of plate
Alkali liquor charging aperture, is that 20%NaOH is molten by 2% addition weight percent concentration of feed weight
Liquid, excludes the impurity such as water and propenyl, propionitrile, Cyanogran. from vacuum distillation tower tower reactor.Thick second
With weight in nitrile, containing acetonitrile 50%, hydrocyanic acid 1.5%.Essence through above flow process
System, in finished product acetonitrile, hydrocyanic acid is 2ppm.
【Embodiment 3】
On the basis of comparative example 1, increase alkali liquor charging after vacuum distillation tower return valve
Mixing mouth, is 20%NaOH solution by 2% addition weight percent concentration of feed weight, from
Vacuum distillation tower tower reactor excludes the impurity such as water and propenyl, propionitrile, Cyanogran..In crude acetonitrile with
Weight, containing acetonitrile 50%, hydrocyanic acid 1.5%.Refined through above flow process, alkali
Liquid directly entered from refluxing opening after being mixed with backflow, it is to avoid increase opening on tower,
In the finished product acetonitrile obtaining, hydrocyanic acid is 2ppm.
【Comparative example 1】
With weight, the raw material crude acetonitrile containing acetonitrile 50%, hydrocyanic acid 1.5%, from
The middle part of dehydrogenation cyanic acid tower adds, and operating pressure is normal pressure, and tower top temperature is 50 DEG C, tower reactor temperature
Spend for 115 DEG C, stripping section lateral line withdrawal function temperature is 92 DEG C.Removed overhead hydrocyanic acid, stripping section
Lateral line withdrawal function concentration is that 75% acetonitrile goes chemical treatment, by total cyanogen: alkali mol ratio is：1∶2.0
Add 40%NaOH solution reaction 4～6 hours.Vacuum distillation tower decompression is entered after chemical treatment
Dehydration and distillation under pressure tower pressurizing and dehydrating, vacuum distillation pressure tower is 0.026Mpa, top temperature 40
DEG C, 64 DEG C of kettle temperature, from vacuum distillation tower tower reactor exclude the impurity such as water and propenyl, propionitrile.Plus
Pressure column pressure is 0.3MPa, and top warm 108 DEG C, 125 DEG C of kettle temperature, from distillation under pressure tower side line
Obtain finished product acetonitrile.Refined through above flow process, hydrocyanic acid 50ppm in finished product acetonitrile.
From the result of above-described embodiment, according to Microamounts of Hydrogen in the acetonitrile refining system of the present invention
The removal methods of cyanic acid, can not increase any complexity chemical treating process and without
Any equipment even in the case of interface on minimizing equipment, by easy method, effectively
Reduce the content of the micro HCN in acetonitrile product.
Claims (15)
1. in a kind of high-purity acetonitrile refining micro hydrocyanic acid removal methods, with from containing acetonitrile,
Continuous recovery high-purity acetonitrile in water, the raw material crude acetonitrile of light component, HCN and weight Organic substance, should
Method comprises the following steps：
A) described raw material crude acetonitrile is delivered in the first knockout tower, by Light ends and major part
HCN is discharged by the tower top of described first knockout tower, by part water and weight Organic substance by described first
The tower reactor of knockout tower is discharged, and takes out from the stripping section bottom side line gas phase of described first knockout tower
Go out containing water-acetonitrile；
B) it is delivered to described chemical treatment kettle containing water-acetonitrile and carries out plus alkali chemical treatment, to remove
Free HCN, thus obtain reactant liquor acetonitrile；
C) described reactant liquor acetonitrile is delivered to the second knockout tower of decompression, in this second knockout tower
Any plate position of rectifying section at or overhead reflux liquid porch add alkali liquor, this second separate
The tower reactor removing weight Organic substance of tower, and second separate tower top and steam and be stripped of most of water from this
Acetonitrile；And
D) the described acetonitrile being stripped of most of water is delivered to the 3rd knockout tower of pressurization, makes this
The second knockout tower is partly returned after the aqueous acetonitrile material condensation that the tower top of the 3rd knockout tower steams
Charging, and extract described high-purity acetonitrile out from the stripping pars infrasegmentalis gas phase of the 3rd knockout tower.
2. method according to claim 1, wherein, in described first knockout tower, tower
Pressure on top surface is 0.10～0.125MPa, and feeding temperature is 30～80 DEG C, and tower top drop temperature is
35～60 DEG C, stripping section lateral line withdrawal function temperature is 85～100 DEG C, and bottom temperature is 105～120
℃.
3. method according to claim 1, wherein, in described second knockout tower, tower
Pressure on top surface is 0.013～0.040Mpa, and feeding temperature is 30～50 DEG C, and tower top temperature is 30～50
DEG C, bottom temperature is 50～75 DEG C.
4. method according to claim 1, wherein, described alkali liquor is alkali metal hydroxide
Thing or the aqueous solution of alkaline earth metal hydroxide.
5. method according to claim 4, wherein, described alkali metal hydroxide or alkali
Earth metal hydroxide is sodium hydroxide, potassium hydroxide or calcium hydroxide.
6. method according to claim 5, wherein, described alkali metal hydroxide or alkali
Earth metal hydroxide is sodium hydroxide.
7. method according to claim 1, wherein, the concentration of described alkali liquor is 1～40
Wt%.
8. method according to claim 7, wherein, the concentration of described alkali liquor is 10～20
Wt%.
9. method according to claim 1, wherein, the mass flow of described alkali liquor is to add
Enter described second knockout tower the mass flow of described reactant liquor acetonitrile 1～10%.
10. method according to claim 9, wherein, the mass flow of described alkali liquor is
Add described second knockout tower the mass flow of described reactant liquor acetonitrile 1～5%.
11. methods according to claim 10, wherein, the mass flow of described alkali liquor is
Add described second knockout tower the mass flow of described reactant liquor acetonitrile 2～3%.
12. methods according to claim 1, wherein, for adding the alkali of described alkali liquor
Liquid charging aperture is located at the plate position of more than the plate position at charging aperture place of described second knockout tower.
13. methods according to claim 12, wherein, described alkali liquor charging aperture is located at institute
State the tower top of the second knockout tower to tower top down to any plate position of charging aperture 10% column plate at.
14. methods according to claim 12, wherein, through described overhead reflux liquid entrance
Add described alkali liquor.
15. methods according to claim 1, wherein, in described 3rd knockout tower,
Tower top pressure is 0.1～0.5MPa, and feeding temperature is 30～90 DEG C, and tower top temperature is 90～140
DEG C, stripping section lateral line withdrawal function temperature is 100～135 DEG C, and bottom temperature is 110～145 DEG C.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510532801.7A CN106478455A (en) | 2015-08-26 | 2015-08-26 | The removal methods of micro hydrocyanic acid in acetonitrile refining system |
| TW105127578A TWI740840B (en) | 2015-08-26 | 2016-08-26 | Acetonitrile refining method, acetonitrile refining system and acid waste water reuse method |
| KR1020160109226A KR102256553B1 (en) | 2015-08-26 | 2016-08-26 | Method for refining acetonitrile, system thereof, and method for reutilizing acid waste water |
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| CN201510532801.7A CN106478455A (en) | 2015-08-26 | 2015-08-26 | The removal methods of micro hydrocyanic acid in acetonitrile refining system |
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| CN106478455A true CN106478455A (en) | 2017-03-08 |
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| CN201510532801.7A Pending CN106478455A (en) | 2015-08-26 | 2015-08-26 | The removal methods of micro hydrocyanic acid in acetonitrile refining system |
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Cited By (2)
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| CN108033900A (en) * | 2017-12-25 | 2018-05-15 | 惠州市宙邦化工有限公司 | A kind of discoloration method of three nitrile of 1,3,6- hexanes |
| CN114773228A (en) * | 2022-04-29 | 2022-07-22 | 河南新邦化工技术有限公司 | Method for refining acetonitrile by rectification-melt crystallization coupling process |
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| CN1328993A (en) * | 2000-06-15 | 2002-01-02 | 中国石油化工集团公司 | Method for removing micro hydrocyanic acid in the course of refining high-purity acetonitrile |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108033900A (en) * | 2017-12-25 | 2018-05-15 | 惠州市宙邦化工有限公司 | A kind of discoloration method of three nitrile of 1,3,6- hexanes |
| CN114773228A (en) * | 2022-04-29 | 2022-07-22 | 河南新邦化工技术有限公司 | Method for refining acetonitrile by rectification-melt crystallization coupling process |
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Application publication date: 20170308 |
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