CN105481716A - Allyl acetonitrile synthesis method and system thereof - Google Patents
Allyl acetonitrile synthesis method and system thereof Download PDFInfo
- Publication number
- CN105481716A CN105481716A CN201510884375.3A CN201510884375A CN105481716A CN 105481716 A CN105481716 A CN 105481716A CN 201510884375 A CN201510884375 A CN 201510884375A CN 105481716 A CN105481716 A CN 105481716A
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- CN
- China
- Prior art keywords
- divinyl
- pentenenitrile
- separation system
- tower separation
- butadiene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/08—Preparation of carboxylic acid nitriles by addition of hydrogen cyanide or salts thereof to unsaturated compounds
- C07C253/10—Preparation of carboxylic acid nitriles by addition of hydrogen cyanide or salts thereof to unsaturated compounds to compounds containing carbon-to-carbon double bonds
Abstract
An allyl acetonitrile synthesis method comprises the following steps: 1, charged liquid butadiene is divided into a liquid part and a gas part; 2, the gasified butadiene part obtained in step 1 is mixed with gaseous butadiene recovered from the top of a tower separation system, and the obtained butadiene mixture is sent to a compressor system and is pressurized; 3, the pressurized gasous butadiene obtained in step 2 is sent to a reaction system in an undersurface bubbling charging mode; and 4, a material obtained after the reaction is sent to the tower separation system from the reaction system through a pump, gaseous butadiene is extracted from the top of the tower separation system, the gasified butadiene part recovered from the top of the tower separation system is used in the process for mixing with the gaseous butadiene part obtained in step, the obtained mixture is sent to the compressor system and is the pressurized, and the allyl acetonitrile product is extracted from the bottom of the tower separation system. The method improves the hydrocyanic acid reaction efficiency, effectively recycles excess butadiene obtained after original emptying, reduces the production cost, protects environment safety, solves the machine sealing problem existing in the installation process of a stirrer, reduces shutdown maintenance, and improves the manual operation safety.
Description
Technical field
The invention belongs to chemical production technical field, particularly relate to a kind of pentenenitrile synthetic process and system.
Background technology
Adiponitrile (ADN, adiponitrile), water white oily liquids, has slight bitter taste, inflammable, molecular formula NC (CH
2)
4cN, density is 962kg/m3, fusing point 1 DEG C, boiling point 295 DEG C.Toxic and corrodibility, sucked by oral cavity or skin absorb all can cause poisoning.Be dissolved in methyl alcohol, ethanol, chloroform, be insoluble in water, hexanaphthene, ether, dithiocarbonic anhydride, tetracol phenixin.Hexanediamine is produced in the main application of adiponitrile, and also there is wide application in this external electronics, light industry and other organic synthesis field.
The operational path of adiponitrile mainly contains vinyl cyanide (AN) Electrolytic Dimeric method, divinyl (BD) hydrocyanation process, hexanodioic acid (ADA) catalytic ammoniation method and hexanolactam and to degrade hydrolysis method again.In the world today, the main technique of adiponitrile suitability for industrialized production is Electrolytic Dimeric Acrylonitrile method and divinyl hydrocyanation process.The reaction that the direct hydrocyanation process of divinyl produces adiponitrile comprises one-level cyaniding, isomerization, secondary cyaniding three steps, the method adopts transition-metal catalyst, two molecular hydrogen cyanic acid are introduced divinyl, and catalyzer adopts the complex compound of the transition metal such as Ni, Rh, Ru usually.Wherein pentenenitrile (3PN) is its important intermediate, and reaction equation is as follows:
One-level cyaniding:
Isomerization:
Secondary cyaniding:
General equation: CH
2=CHCH=CH
2+ 2HCN → NC (CH
2)
4cN+4H
2
One-level cyaniding is produced in the process of pentenenitrile (3PN), the autohemagglutination of HCN is often there is in BD and HCN reaction process, cause the blocking of pipeline and equipment, and HCN is as highly toxic substance, maintenance shut-downs process can cause very large potential safety hazard to workman, therefore be necessary to increase BD and HCN mixedness, improve HCN speed of reaction, prevent from keeping in repair the leakage intoxication accident caused, simultaneously circulation and stress BD, save high raw materials cost, meet the requirement that environment-friendly enterprise is produced simultaneously.
Summary of the invention
The object of the invention is to solve in the process of producing pentenenitrile, the autohemagglutination of prussic acid occurs in divinyl and prussic acid reaction process, and cause the blocking of pipeline and equipment, maintenance shut-downs process can cause the problem of very large potential safety hazard to workman.The concrete technical scheme adopted is as follows:
A kind of pentenenitrile synthetic process, comprises the steps:
Step 1: liquid phase butadiene feed is divided into two portions, a part directly enters reactive system and mixes with prussic acid, and another part gasifies;
Step 2: by the gas phase divinyl of the gasifying section of divinyl described in step 1 and tower separation system recovered overhead, sends into compressor assembly pressurization after mixing;
Step 3: the gas phase divinyl after step 3 being pressurizeed is sent in reactive system with bubbling feeding manner under liquid;
Step 4: reacting rear material sends into tower separation system through pump by reactive system, overhead extraction gas phase divinyl, as as described in step 2, by the gas phase divinyl of the gasifying section of divinyl described in step 1 and tower separation system recovered overhead, compressor assembly pressurization is sent into, extraction pentenenitrile product at the bottom of tower after mixing.
Described in step 1, liquid phase butadiene feed is divided into two portions, and liquid phase part and gas phase portion mass ratio are 3:1.
Gas phase divinyl and the gasifying section of divinyl described in step 1 of tower separation system recovered overhead described in step 2 need before mixing to lower the temperature through condenser system to process.Through condenser system, temperature is reduced to 5 DEG C ~ 15 DEG C.
Described in step 2, compressor assembly is pressurized to 20 ~ 50KpaG.
A kind of pentenenitrile synthesis system, liquid phase butadiene feed end is connected with reactive system and divinyl gasification system respectively, tower separation system top exit and divinyl gasification system export and are jointly connected to compressor assembly, compressor assembly outlet is connected to bottom reactive system, reactive system is provided with catalyst inlet and prussic acid entrance, reactive system is connected by pump with tower separation system, is provided with pentenenitrile products export bottom tower separation system.
Tower separation system is connected by condenser system with between compressor assembly.
Described reactive system is reactor, and described tower separation system is rectifying tower group.
The invention has the beneficial effects as follows: gas-liquid two strands of divinyl materials mix with prussic acid by processing method of the present invention, improve prussic acid reaction efficiency.The excess butadiene that original emptying is discharged by reaction process carries out effective recycling, reduces production cost, protects environmental safety.Reactive system is operated by bubbling and replaces conventional agitator married operation, solves during agitator is installed the mechanical seal problem existed, ensures highly toxic substance closed-loop operation as far as possible, reduce maintenance shut-downs, improve manually-operated security.The invention of novel technological method meets requirement that is environmentally friendly, production safety type enterprise.
Accompanying drawing explanation
Fig. 1 is pentenenitrile synthetic process process flow sheet of the present invention
Marginal data: 1, reactive system, 2, tower separation system, 3, compressor assembly, 4, condenser system, 5, pump, 6, divinyl gasification system
A, liquid phase divinyl, B, catalyzer, C, prussic acid, D, pentenenitrile
Embodiment
The technique means realized to make the present invention, creation characteristic, reach object and effect is easy to understand; below the specific embodiment of the present invention is described further; but do not limit protection scope of the present invention; it should be noted that; when not conflicting, the embodiment in the invention and the feature in embodiment can combine mutually.
Pentenenitrile synthesis system of the present invention, syndeton is: liquid phase divinyl A feed end is connected with reactive system 1 and divinyl gasification system 6 respectively, tower separation system 2 top exit and divinyl gasification system 6 export and are jointly connected to compressor assembly 3, compressor assembly 3 outlet is connected to bottom reactive system 1, reactive system 1 is provided with catalyst B entrance and prussic acid C entrance, reactive system 1 is connected by pump 5 with tower separation system 2, is provided with pentenenitrile D products export bottom tower separation system 2.Be connected by condenser system 4 between tower separation system 2 with compressor assembly 3.
Described reactive system 1 is reactor, and described tower separation system 2 is rectifying tower group.
Embodiment 1:
Liquid phase divinyl A input speed is 8000kg/h, two portions are divided to export, a part is directly sent into reactive system 1 with 6000kg/h and is mixed with prussic acid C, another part gasifies with 2000kg/h speed, and send into compressor assembly 3 after mixing with the gas phase divinyl of tower separation system 2 recovered overhead and be forced into 20KpaG, and send in reactive system 1 with bubbling feeding manner under liquid, reacting rear material sends into tower separation system 2 through pump 5 by reactive system 1, overhead extraction gas phase divinyl, 5 DEG C are cooled to through condenser system 4, as abovementioned steps, compressor assembly 3 is sent into after the gasifying section that this partial gas phase divinyl and liquid phase divinyl A opening for feed separate mixes, finally extraction pentenenitrile D product at the bottom of tower separation system 2 tower.
Embodiment 2:
Liquid phase divinyl A input speed is 12000kg/h, two portions are divided to export, a part is directly sent into reactive system 1 with 9000kg/h and is mixed with prussic acid C, another part gasifies with 3000kg/h speed, and send into compressor assembly 3 after mixing with the gas phase divinyl of tower separation system 2 recovered overhead and be forced into 35KpaG, and send in reactive system 1 with bubbling feeding manner under liquid, reacting rear material sends into tower separation system 2 through pump 5 by reactive system 1, overhead extraction gas phase divinyl, 10 DEG C are cooled to through condenser system 4, as abovementioned steps, compressor assembly 3 is sent into after the gasifying section that this partial gas phase divinyl and liquid phase divinyl A opening for feed separate mixes, finally extraction pentenenitrile D product at the bottom of tower separation system 2 tower.
Embodiment 3:
Liquid phase divinyl A input speed is 16000kg/h, two portions are divided to export, a part is directly sent into reactive system 1 with 12000kg/h and is mixed with prussic acid C, another part gasifies with 4000kg/h speed, and send into compressor assembly 3 after mixing with the gas phase divinyl of tower separation system 2 recovered overhead and be forced into 50KpaG, and send in reactive system 1 with bubbling feeding manner under liquid, reacting rear material sends into tower separation system 2 through pump 5 by reactive system 1, overhead extraction gas phase divinyl, 15 DEG C are cooled to through condenser system 4, as abovementioned steps, compressor assembly 3 is sent into after the gasifying section that this partial gas phase divinyl and liquid phase divinyl A opening for feed separate mixes, finally extraction pentenenitrile D product at the bottom of tower separation system 2 tower.
Comparative example:
Comparative example uses traditional pentenenitrile production technique, stirs reactive system with agitator, produces pentenenitrile.
Above-mentioned is the embodiment 1-3 using present invention process and system to carry out pentenenitrile production, and using traditional method to carry out the comparative example of pentenenitrile production, the contrast consumed the discharge of its divinyl, maintenance intervals, raw materials cost consumption, cost of labor is as shown in Table 1.
Table 1 embodiment and comparative example effect comparison table
The present invention is directed to conventional art by table 1 is known to have maintenance cost low, material equipment cost consumption is low, and cost of labor consumption is a little few, and is also significantly less than traditional technology to the discharge of divinyl.
Processing method of the present invention and system are described by specific embodiment.Those skilled in the art can use for reference content appropriate change conversion unit of the present invention; the links such as reaction parameter realize other object corresponding; its relevant change does not all depart from content of the present invention; within all spirit in the invention and principle; any amendment of doing, equivalent replacement, improvement etc., within the protection domain that all should be included in the invention.
Claims (9)
1. a pentenenitrile synthetic process, is characterized in that, comprises the steps:
Step 1: liquid phase butadiene feed is divided into two portions, a part directly enters reactive system and mixes with prussic acid, and another part gasifies;
Step 2: by the gas phase divinyl of the gasifying section of divinyl described in step 1 and tower separation system recovered overhead, sends into compressor assembly pressurization after mixing;
Step 3: the gas phase divinyl after step 3 being pressurizeed is sent in reactive system with bubbling feeding manner under liquid;
Step 4: reacting rear material sends into tower separation system through pump by reactive system, overhead extraction gas phase divinyl, as as described in step 2, by the gas phase divinyl of the gasifying section of divinyl described in step 1 and tower separation system recovered overhead, compressor assembly pressurization is sent into, extraction pentenenitrile product at the bottom of tower after mixing.
2. a kind of pentenenitrile synthetic process according to claim 1, is characterized in that, gas phase divinyl and the gasifying section of divinyl described in step 1 of tower separation system recovered overhead described in step 2 need before mixing to lower the temperature through condenser system to process.
3. a kind of pentenenitrile synthetic process according to claim 2, is characterized in that, through condenser system, temperature is reduced to 5 DEG C ~ 15 DEG C.
4. a kind of pentenenitrile synthetic process according to claim 1, it is characterized in that, described in step 1, liquid phase butadiene feed is divided into two portions, and liquid phase part and gas phase portion mass ratio are 3:1.
5. a kind of pentenenitrile synthetic process according to claim 1, it is characterized in that, described in step 2, compressor assembly is pressurized to 20 ~ 50KpaG.
6. a pentenenitrile synthesis system, it is characterized in that, liquid phase butadiene feed end is connected with reactive system and divinyl gasification system respectively, tower separation system top exit and divinyl gasification system export and are jointly connected to compressor assembly, compressor assembly outlet is connected to bottom reactive system, reactive system is provided with catalyst inlet and prussic acid entrance, and reactive system is connected by pump with tower separation system, is provided with pentenenitrile products export bottom tower separation system.
7. a kind of pentenenitrile synthesis system according to claim 6, it is characterized in that, tower separation system is connected by condenser system with between compressor assembly.
8. a kind of pentenenitrile synthesis system according to claim 6, is characterized in that, described reactive system is reactor.
9. a kind of pentenenitrile synthesis system according to claim 6, is characterized in that, described tower separation system is rectifying tower group.
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| CN201510884375.3A CN105481716B (en) | 2015-12-04 | 2015-12-04 | A kind of allyl acetonitrile synthetic process and system |
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| CN201510884375.3A CN105481716B (en) | 2015-12-04 | 2015-12-04 | A kind of allyl acetonitrile synthetic process and system |
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| CN105481716A true CN105481716A (en) | 2016-04-13 |
| CN105481716B CN105481716B (en) | 2018-04-27 |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005073171A1 (en) * | 2004-01-29 | 2005-08-11 | Basf Aktiengesellschaft | Method for producing 3-pentenenitrile |
| CN1914155A (en) * | 2004-01-29 | 2007-02-14 | 巴斯福股份公司 | Method for the hydrocyanation of butadiene |
| CN205275496U (en) * | 2015-12-04 | 2016-06-01 | 中国天辰工程有限公司 | Allyl acetonitrile synthesis system |
-
2015
- 2015-12-04 CN CN201510884375.3A patent/CN105481716B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005073171A1 (en) * | 2004-01-29 | 2005-08-11 | Basf Aktiengesellschaft | Method for producing 3-pentenenitrile |
| CN1914155A (en) * | 2004-01-29 | 2007-02-14 | 巴斯福股份公司 | Method for the hydrocyanation of butadiene |
| CN205275496U (en) * | 2015-12-04 | 2016-06-01 | 中国天辰工程有限公司 | Allyl acetonitrile synthesis system |
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| CN105481716B (en) | 2018-04-27 |
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