CN101747245B - Process for preparing N, N-diethyltrifluoromethanesulfonamide CF3SO2N (C2H5)2from trifluoromethanesulfonyl fluoride - Google Patents

Process for preparing N, N-diethyltrifluoromethanesulfonamide CF3SO2N (C2H5)2from trifluoromethanesulfonyl fluoride Download PDF

Info

Publication number
CN101747245B
CN101747245B CN2008102436289A CN200810243628A CN101747245B CN 101747245 B CN101747245 B CN 101747245B CN 2008102436289 A CN2008102436289 A CN 2008102436289A CN 200810243628 A CN200810243628 A CN 200810243628A CN 101747245 B CN101747245 B CN 101747245B
Authority
CN
China
Prior art keywords
fluoride sulfonyl
trimethyl fluoride
liquid
diethyl
dehydration
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN2008102436289A
Other languages
Chinese (zh)
Other versions
CN101747245A (en
Inventor
许文林
陶荣辉
王雅琼
徐晓强
司宗飞
陈晓荣
丁培兴
李霞
王一明
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
JIANGSU GUOTAI SUPER POWER NEW MATERIALS Co Ltd
Original Assignee
Yangzhou University
Zhangjiagang Guotai Huarong New Chemical Materials Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Yangzhou University, Zhangjiagang Guotai Huarong New Chemical Materials Co Ltd filed Critical Yangzhou University
Priority to CN2008102436289A priority Critical patent/CN101747245B/en
Publication of CN101747245A publication Critical patent/CN101747245A/en
Application granted granted Critical
Publication of CN101747245B publication Critical patent/CN101747245B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/582—Recycling of unreacted starting or intermediate materials

Landscapes

  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention relates to a method for preparing N, N-diethyl trifluoro-methanesulfonyl fluoride CF3SO2N (C2H5)2 by using trifluoro-methanesulfonyl fluoride N, which comprises the following steps: firstly, adding the trifluoro-methanesulfonyl fluoride CF3SO2F into diethylamine (C2H5) 2NH and carrying out chemical absorption to the trifluoro-methanesulfonyl fluoride CF3SO2F; secondly, evaporating; thirdly, adding water H2O in a liquid-phase product obtained by evaporation to mix and extract; fourthly, carrying out liquid-liquid separation to materials after being mixed and extracted and causing oil phase to enter the next step; fifthly, removing impurities and dewatering; sixthly, carrying out solid-liquid separation to materials obtained from the previous step, therefore, liquid phase is the obtained product, that is, N, namely the N-diethyl trifluoro-methanesulfonyl fluoride CF3SO2N (C2H5)2. The invention has the advantages of easily obtainable raw materials, simple separation process, less power consumption, good product quality, high yield, low cost, cleanness and environment protection.

Description

The trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method
Technical field
The present invention relates to a kind of N of preparation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, particularly a kind of trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, belong to the fine chemical technology field.
Background technology
N, N-diethyl trimethyl fluoride sulfonyl amine, molecular formula is CF 3SO 2N (C 2H 5) 2, molecular weight is 205, boiling point is 168-170 ℃ (760mmHg), 55 ℃ (7mmHg) is flowable brown color liquid under the normal temperature, is slightly soluble in water, easy molten ethanol, acetone, DMC, PC etc. are mainly used in the raw material that fine chemistry industry is synthetic and ionogen prepares.
Trimethyl fluoride sulfonyl fluorine, molecular formula are CF 3SO 2F is brown gas under the normal temperature, about b.p:-21 ℃, is slightly soluble in water, is dissolved in the organic solvent, and reactive behavior is higher.
Diethylamine, molecular formula are (C 2H 5) 2NH, molecular weight are 73.14, are volatile colourless liquid, and the smell of ammonia is arranged, and fusing point is-38.9 ℃, and boiling point is 55.5 ℃, and specific refractory power is 1.3864, and flash-point is-28 ℃, and density is 0.7056g/cm 3(20 ℃), relative density (air=1) is 2.53, saturation vapour pressure (38 ℃) is 53.32kPa, and the combustion heat is 2996.6kJ/mol, and critical temperature is 223 ℃, emergent pressure is 3.71MPa, the logarithmic value of Octanol/water Partition Coefficients is 1.43～1.57, and ignition temperature is 312 ℃, and upper explosive limit % (V/V) is 10.1, Lower Explosive Limit % (V/V) is 1.7, water-soluble, pure, ether.Can be miscible with water, ethanol, be dissolved in ether, be alkalescence, strong basicity, inflammable, volatile, tool corrodibility, strong and stimulating generate salt soluble in water with inorganic acid reaction, and prohibiting and joining thing is strong oxidizer, acids, chloride of acid, acid anhydrides.Can be used as the intermediate of production medicine, agricultural chemicals, dyestuff, mineral flotation agent, emulsifying agent and fine chemicals etc.
Summary of the invention
The purpose of this invention is to provide that a kind of technique is simple, consuming little energy, good product quality, trimethyl fluoride sulfonyl fluorine that production cost is low prepare N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method.
Realize that the above-mentioned purpose technical scheme is: a kind of trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, be with trimethyl fluoride sulfonyl fluorine CF 3SO 2F is raw material, and described method steps is as follows:
(1) chemical absorption: in absorption equipment, diethylamine (C 2H 5) 2Add trimethyl fluoride sulfonyl fluorine CF among the NH 3SO 2F is to trimethyl fluoride sulfonyl fluorine CF 3SO 2F carries out chemical absorption;
(2) evaporation: the material after the previous step chemical absorption is evaporated the diethylamine (C that the gas-phase product of evaporation obtains through condensation 2H 5) 2NH recycles, and the liquid phase material after the evaporation enters next step;
(3) hybrid extraction: in the liquid phase material that the previous step evaporation obtains, add entry H 2O carries out the hybrid extraction operation;
(4) liquid-liquid separation: the material behind the previous step hybrid extraction is through liquid-liquid separation, and water is diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2The aqueous solution, oil phase are principal product N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Enter next step;
(5) removal of impurities and dehydration: with principal product N obtained in the previous step, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle adding cleaner and dewatering agent carry out removal of impurities and dehydration;
(6) solid-liquid separates: material obtained in the previous step is carried out solid-liquid separate, solid phase further recycles, the product N of liquid phase for obtaining, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2
Further, described the first step chemical absorption equipment is that autoclave stirs any one in chemical reactor, tubular chemical reactor or the chemical absorption tower, operational condition is 20 ℃～80 ℃ of temperature of reaction, reaction absolute pressure 0.1MPa～1.0MPa, trimethyl fluoride sulfonyl fluorine CF 3SO 2F and diethylamine (C 2H 5) 2The mol ratio of NH is 1.0: 5.0～50.0.
Further, the operational condition of described second step evaporation is 20 ℃～55 ℃ of vaporization temperatures, evaporation absolute pressure 0.01MPa～0.1MPa.
Further, in described the 3rd step hybrid extraction, the material and the water H that obtain after the second step evaporation 2The volume ratio of the add-on of O is 1.0: 1.0～10.0.
Further, described the 5th step removal of impurities and dehydration is the rear removal of impurities of dewatering first, or first impurity and then dehydration, or removal of impurities and dehydration are carried out simultaneously.
Further, removal of impurities is the oil phase principal product N that obtains at the 4th step liquid-liquid separation after the described first dehydration, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2The middle dewatering agent that adds first dewaters, and carries out solid-liquid after the dehydration and separates, and adds cleaner again and carry out adsorption-edulcoration in the liquid phase that the solid-liquid separation obtains.
Further, described first impurity and then dehydration is the oil phase principal product N that obtains at the 4th step liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2The middle cleaner that adds first carries out adsorption-edulcoration, carries out solid-liquid behind the adsorption-edulcoration and separates, and adds dewatering agent again and dewater in the liquid phase that the solid-liquid separation obtains.
Further, described removal of impurities and dehydration are carried out simultaneously, are the oil phase principal product N that obtains at the 4th step liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle cleaner and the dewatering agent of adding simultaneously carries out removal of impurities and dehydration.
Further, described dewatering agent is Na 2SO 4, P 2O 5, in activated carbon, diatomite or the molecular sieve any one.
Further, described cleaner is any one in activated carbon, diatomite or the molecular sieve.
Chemical equation of the present invention is:
Figure G2008102436289D00031
Realize that the main technique equipment that the present invention needs is: chemical absorption equipment, hybrid extraction equipment, filter plant etc.
Adopt the benefit of technique scheme to be: (1), the present invention adopt trimethyl fluoride sulfonyl fluorine CF 3SO 2Direct and the diethylamine (C of F 2H 5) 2The NH reaction generates N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2, raw material is easy to get, and sepn process is simple, and raw materials cost is low, and operational path is short, and technique is simple, consuming little energy; (2), take full advantage of the singularity of product and reactant, adopt evaporation to recycle diethylamine (C 2H 5) 2Material N after NH, the evaporation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Be slightly soluble in water and diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2Characteristic extremely soluble in water, at N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2Add entry H in the sepn process of mixture 2O carries out the hybrid extraction operation, has further simplified processing step, has reduced production cost, has improved the security of technological process; (3), realized cleaning production, be convenient to suitability for industrialized production, produce without the three wastes, cleaning, environmental protection, various by products can be recycled, this has saved cost greatly; (4), adopt the product N of processing method preparation of the present invention, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Quality is good, and yield is high, and cost is low.
Description of drawings
Fig. 1 is process flow sheet of the present invention;
Fig. 2 is that the present invention was embodiment one process flow sheet of rear removal of impurities that dewaters first in the 5th step;
Fig. 3 is that the present invention was embodiment two process flow sheets of first impurity and then dehydration in the 5th step;
Fig. 4 is that the present invention was removal of impurities and the dewater embodiment three that carries out simultaneously, four and five process flow sheet in the 5th step.
Embodiment
The present invention is further detailed explanation below in conjunction with drawings and Examples.
Embodiment one
Major equipment: autoclave stirs chemical reactor, hybrid extraction equipment, filter plant.
Main raw material: trimethyl fluoride sulfonyl fluorine CF 3SO 2F, diethylamine (C 2H 5) 2NH, dewatering agent Na 2SO 4, the cleaner molecular sieve.
As depicted in figs. 1 and 2, a kind of trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, be with trimethyl fluoride sulfonyl fluorine CF 3SO 2F is raw material, and described method steps is as follows:
(1) chemical absorption: stir in the chemical reactor diethylamine (C in autoclave 2H 5) 2Add trimethyl fluoride sulfonyl fluorine CF among the NH 3SO 2F is to trimethyl fluoride sulfonyl fluorine CF 3SO 2F carries out chemical absorption, and operational condition is 20 ℃ of temperature of reaction, reaction absolute pressure 0.1MPa, trimethyl fluoride sulfonyl fluorine CF 3SO 2F and diethylamine (C 2H 5) 2The mol ratio of NH is 1.0: 50.0;
(2) evaporation: the material after the previous step chemical absorption is evaporated, and operational condition is 20 ℃ of vaporization temperatures, evaporation absolute pressure 0.01MPa, the diethylamine (C that the gas-phase product of evaporation obtains through condensation 2H 5) 2NH recycles, the material N after the evaporation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2Enter next step;
(3) hybrid extraction: in hybrid extraction equipment, with the liquid product N that the previous step evaporation obtains, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2In add entry H 2O carries out the hybrid extraction operation under the room temperature, the material and the water H that obtain after the second step evaporation 2The volume ratio of the add-on of O is 1.0: 1.0;
(4) liquid-liquid separation: the material behind the previous step hybrid extraction is through liquid-liquid separation, and water is diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2The aqueous solution, oil phase are principal product N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Enter next step;
(5) removal of impurities and dehydration: with principal product N obtained in the previous step, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle adding cleaner and dewatering agent carry out removal of impurities and dehydration, and removal of impurities and dehydration sequentially are the rear removal of impurities of dewatering first, and removal of impurities is the oil phase principal product N that obtains at the 4th step liquid-liquid separation after the described first dehydration, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2The middle dewatering agent Na that adds first 2SO 4Dewater, generate Na 2SO 4NH 2O adds dewatering agent Na 2SO 4Amount be 1% of the oil phase material amount that obtained behind the liquid-liquid separation in the 4th step, carry out solid-liquid after the dehydration and separate the solid phase Na that obtains 2SO 4NH 2O goes further recycling, and the liquid phase that obtains is the N that contains impurity, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2, in the liquid phase that the solid-liquid separation obtains, add again the cleaner molecular sieve and carry out adsorption-edulcoration;
(6) solid-liquid separates: in filter plant, material obtained in the previous step is carried out solid-liquid separate, solid phase is that cleaner and impurity go further recycling, the product N of liquid phase for obtaining, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2
Embodiment two
Major equipment: tubular chemical reactor, hybrid extraction equipment, filter plant.
Main raw material: trimethyl fluoride sulfonyl fluorine CF 3SO 2F, diethylamine (C 2H 5) 2NH, dewatering agent P 2O 5, the cleaner activated carbon.
As shown in figures 1 and 3, a kind of trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, be with trimethyl fluoride sulfonyl fluorine CF 3SO 2F is raw material, and described method steps is as follows:
(1) chemical absorption: in tubular chemical reactor, diethylamine (C 2H 5) 2Add trimethyl fluoride sulfonyl fluorine CF among the NH 3SO 2F is to trimethyl fluoride sulfonyl fluorine CF 3SO 2F carries out chemical absorption, and operational condition is 60 ℃ of temperature of reaction, reaction absolute pressure 0.5MPa, trimethyl fluoride sulfonyl fluorine CF 3SO 2F and diethylamine (C 2H 5) 2The mol ratio of NH is 1.0: 20.0;
(2) evaporation: the material after the previous step chemical absorption is evaporated, and operational condition is 40 ℃ of vaporization temperatures, evaporation absolute pressure 0.08MPa, the diethylamine (C that the gas-phase product of evaporation obtains through condensation 2H 5) 2NH recycles, the material N after the evaporation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2Enter next step;
(3) hybrid extraction: in hybrid extraction equipment, with the liquid product N that the previous step evaporation obtains, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2In add entry H 2O carries out the hybrid extraction operation under the room temperature, the material and the water H that obtain after the second step evaporation 2The volume ratio of the add-on of O is 1.0: 3.0;
(4) liquid-liquid separation: the material behind the previous step hybrid extraction is through liquid-liquid separation, and water is diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2The aqueous solution, oil phase are principal product N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Enter next step;
(5) removal of impurities and dehydration: with principal product N obtained in the previous step, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle adding cleaner and dewatering agent carry out removal of impurities and dehydration, and removal of impurities and dehydration sequentially are first impurity and then dehydration, and described first impurity and then dehydration is the oil phase principal product N that obtains at the 4th step liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2The middle cleaner activated carbon that adds first carries out adsorption-edulcoration, the amount that adds the cleaner activated carbon is 3% of the oil phase material amount that obtains behind the 4th step liquid-liquid separation, carry out solid-liquid behind the adsorption-edulcoration and separate, the solid phase that obtains is that cleaner and impurity go further recycling, contains H 2The N of O, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Add again dewatering agent P in the liquid phase 2O 5Dewater, the amount that adds the cleaner activated carbon is 2% of the oil phase material amount that obtains behind the 4th step liquid-liquid separation;
(6) solid-liquid separates: in filter plant, material obtained in the previous step is carried out solid-liquid separate, solid phase is that dewatering agent and impurity go further recycling, the product N of liquid phase for obtaining, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2
Embodiment three
Major equipment: chemical absorption tower, hybrid extraction equipment, filter plant.
Main raw material: trimethyl fluoride sulfonyl fluorine CF 3SO 2F, diethylamine (C 2H 5) 2NH, dewatering agent diatomite, cleaner diatomite.
As shown in Figure 1 and Figure 4, a kind of trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, be with trimethyl fluoride sulfonyl fluorine CF 3SO 2F is raw material, and described method steps is as follows:
(1) chemical absorption: in the chemical absorption tower, diethylamine (C 2H 5) 2Add trimethyl fluoride sulfonyl fluorine CF among the NH 3SO 2F is to trimethyl fluoride sulfonyl fluorine CF 3SO 2F carries out chemical absorption, and operational condition is 80 ℃ of temperature of reaction, reaction absolute pressure 1.0MPa, trimethyl fluoride sulfonyl fluorine CF 3SO 2F and diethylamine (C 2H 5) 2The mol ratio of NH is 1.0: 5.0;
(2) evaporation: the material after the previous step chemical absorption is evaporated, and operational condition is 55 ℃ of vaporization temperatures, evaporation absolute pressure 0.1MPa, the diethylamine (C that the gas-phase product of evaporation obtains through condensation 2H 5) 2NH recycles, the material N after the evaporation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2Enter next step;
(3) hybrid extraction: in hybrid extraction equipment, with the liquid product N that the previous step evaporation obtains, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2In add entry H 2O carries out the hybrid extraction operation under the room temperature, the material and the water H that obtain after the second step evaporation 2The volume ratio of the add-on of O is 1.0: 10.0;
(4) liquid-liquid separation: the material behind the previous step hybrid extraction is through liquid-liquid separation, and water is diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2The aqueous solution, oil phase are principal product N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Enter next step;
(5) removal of impurities and dehydration: with principal product N obtained in the previous step, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle adding cleaner and dewatering agent carry out removal of impurities and dehydration, and removal of impurities and dehydration sequentially are that removal of impurities and dehydration are carried out simultaneously, and described removal of impurities and dehydration are carried out simultaneously, are the oil phase principal product N that obtains at the 4th step liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle cleaner diatomite and the dewatering agent diatomite of adding simultaneously carries out removal of impurities and dehydration, adds cleaner and the diatomaceous amount of dewatering agent and be 4% of the oil phase material amount that obtains behind the 4th step liquid-liquid separation;
(6) solid-liquid separates: in filter plant, material obtained in the previous step is carried out solid-liquid separate, solid phase is that cleaner, dewatering agent and impurity go further recycling, the product N of liquid phase for obtaining, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2
Embodiment four
Major equipment: autoclave stirs chemical reactor, hybrid extraction equipment, filter plant.
Main raw material: trimethyl fluoride sulfonyl fluorine CF 3SO 2F, diethylamine (C 2H 5) 2NH, dewatering agent molecular sieve, cleaner molecular sieve.
As shown in Figure 1 and Figure 4, a kind of trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, be with trimethyl fluoride sulfonyl fluorine CF 3SO 2F is raw material, and described method steps is as follows:
(1) chemical absorption: stir in the chemical reactor diethylamine (C in autoclave 2H 5) 2Add trimethyl fluoride sulfonyl fluorine CF among the NH 3SO 2F is to trimethyl fluoride sulfonyl fluorine CF 3SO 2F carries out chemical absorption, and operational condition is 40 ℃ of temperature of reaction, reaction absolute pressure 0.3MPa, trimethyl fluoride sulfonyl fluorine CF 3SO 2F and diethylamine (C 2H 5) 2The mol ratio of NH is 1.0: 30.0;
(2) evaporation: the material after the previous step chemical absorption is evaporated, and operational condition is 30 ℃ of vaporization temperatures, evaporation absolute pressure 0.05MPa, the diethylamine (C that the gas-phase product of evaporation obtains through condensation 2H 5) 2NH recycles, the material N after the evaporation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2Enter next step;
(3) hybrid extraction: in hybrid extraction equipment, with the liquid product N that the previous step evaporation obtains, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2In add entry H 2O carries out the hybrid extraction operation under the room temperature, the material and the water H that obtain after the second step evaporation 2The volume ratio of the add-on of O is 1.0: 2.0;
(4) liquid-liquid separation: the material behind the previous step hybrid extraction is through liquid-liquid separation, and water is diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2The aqueous solution, oil phase are principal product N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Enter next step;
(5) removal of impurities and dehydration: with principal product N obtained in the previous step, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle adding cleaner and dewatering agent carry out removal of impurities and dehydration, and removal of impurities and dehydration sequentially are that removal of impurities and dehydration are carried out simultaneously, and described removal of impurities and dehydration are carried out simultaneously, are the oil phase principal product N that obtains at the 4th step liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle cleaner molecular sieve and the dewatering agent molecular sieve of adding simultaneously carries out removal of impurities and dehydration;
(6) solid-liquid separates: in filter plant, material obtained in the previous step is carried out solid-liquid separate, solid phase is that cleaner, dewatering agent and impurity go further recycling, the product N of liquid phase for obtaining, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2
Embodiment five
Major equipment: chemical absorption tower, hybrid extraction equipment, filter plant.
Main raw material: trimethyl fluoride sulfonyl fluorine CF 3SO 2F, diethylamine (C 2H 5) 2NH, dewatering agent activated carbon, cleaner activated carbon.
As shown in Figure 1 and Figure 4, a kind of trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, be with trimethyl fluoride sulfonyl fluorine CF 3SO 2F is raw material, and described method steps is as follows:
(1) chemical absorption: in the chemical absorption tower, diethylamine (C 2H 5) 2Add trimethyl fluoride sulfonyl fluorine CF among the NH 3SO 2F is to trimethyl fluoride sulfonyl fluorine CF 3SO 2F carries out chemical absorption, and operational condition is 70 ℃ of temperature of reaction, reaction absolute pressure 0.8MPa, trimethyl fluoride sulfonyl fluorine CF 3SO 2F and diethylamine (C 2H 5) 2The mol ratio of NH is 1.0: 10.0;
(2) evaporation: the material after the previous step chemical absorption is evaporated, and operational condition is 45 ℃ of vaporization temperatures, evaporation absolute pressure 0.09MPa, the diethylamine (C that the gas-phase product of evaporation obtains through condensation 2H 5) 2NH recycles, the material N after the evaporation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2Enter next step;
(3) hybrid extraction: in hybrid extraction equipment, with the liquid product N that the previous step evaporation obtains, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2With diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2In add entry H 2O carries out the hybrid extraction operation under the room temperature, the material and the water H that obtain after the second step evaporation 2The volume ratio of the add-on of O is 1.0: 8.0;
(4) liquid-liquid separation: the material behind the previous step hybrid extraction is through liquid-liquid separation, and water is diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2The aqueous solution, oil phase are principal product N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Enter next step;
(5) removal of impurities and dehydration: with principal product N obtained in the previous step, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle adding cleaner and dewatering agent carry out removal of impurities and dehydration, and removal of impurities and dehydration sequentially are that removal of impurities and dehydration are carried out simultaneously, and described removal of impurities and dehydration are carried out simultaneously, are the oil phase principal product N that obtains at the 4th step liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle cleaner activated carbon and the dewatering agent activated carbon of adding simultaneously carries out removal of impurities and dehydration, and the amount that adds cleaner and dewatering agent activated carbon is 3% of the oil phase material amount that obtains behind the 4th step liquid-liquid separation;
(6) solid-liquid separates: in filter plant, material obtained in the previous step is carried out solid-liquid separate, solid phase is that cleaner, dewatering agent and impurity go further recycling, the product N of liquid phase for obtaining, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2
Except the various embodiments described above, embodiment of the present invention also have a lot, and the technical scheme that all employings are equal to or equivalence is replaced is all within protection scope of the present invention.

Claims (9)

1. a trimethyl fluoride sulfonyl fluorine prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, be with trimethyl fluoride sulfonyl fluorine CF 3SO 2F is raw material, it is characterized in that described method steps is as follows:
(1) chemical absorption: in absorption equipment, diethylamine (C 2H 5) 2Add trimethyl fluoride sulfonyl fluorine CF among the NH 3SO 2F is to trimethyl fluoride sulfonyl fluorine CF 3SO 2F carries out chemical absorption;
(2) evaporation: the material after the previous step chemical absorption is evaporated the diethylamine (C that the gas-phase product of evaporation obtains through condensation 2H 5) 2NH recycles, and the liquid phase material after the evaporation enters next step;
(3) hybrid extraction: in the liquid phase material that the previous step evaporation obtains, add entry H 2O carries out the hybrid extraction operation;
(4) liquid-liquid separation: the material behind the previous step hybrid extraction is through liquid-liquid separation, and water is diethylamine hydrogen fluoride salts HFHN (C 2H 5) 2The aqueous solution, oil phase are principal product N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Enter next step;
(5) removal of impurities and dehydration: with principal product N obtained in the previous step, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle adding cleaner and dewatering agent carry out removal of impurities and dehydration, and described this step removal of impurities and dehydration are the rear removal of impurities of dewatering first, or first impurity and then dehydration, or removal of impurities and dehydration are carried out simultaneously;
(6) solid-liquid separates: material obtained in the previous step is carried out solid-liquid separate, solid phase further recycles, the product N of liquid phase for obtaining, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2
2. trimethyl fluoride sulfonyl fluorine according to claim 1 prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, it is characterized in that: described the first step chemical absorption equipment is that autoclave stirs any one in chemical reactor, tubular chemical reactor or the chemical absorption tower, operational condition is 20 ℃～80 ℃ of temperature of reaction, reaction absolute pressure 0.1MPa～1.0MPa, trimethyl fluoride sulfonyl fluorine CF 3SO 2F and diethylamine (C 2H 5) 2The mol ratio of NH is 1.0: 5.0～50.0.
3. trimethyl fluoride sulfonyl fluorine according to claim 1 prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, it is characterized in that: the operational condition of described second step evaporation is 20 ℃～55 ℃ of vaporization temperatures, evaporation absolute pressure 0.01MPa～0.1MPa.
4. trimethyl fluoride sulfonyl fluorine according to claim 1 prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, it is characterized in that: in described the 3rd step hybrid extraction, the material and the water H that obtain after the second step evaporation 2The volume ratio of the add-on of O is 1.0: 1.0～10.0.
5. trimethyl fluoride sulfonyl fluorine according to claim 1 prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, it is characterized in that: removal of impurities is at the 4th step oil phase principal product N that obtain of liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF after the described first dehydration 3SO 2N (C 2H 5) 2The middle dewatering agent that adds first dewaters, and carries out solid-liquid after the dehydration and separates, and adds cleaner again and carry out adsorption-edulcoration in the liquid phase that the solid-liquid separation obtains.
6. trimethyl fluoride sulfonyl fluorine according to claim 1 prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, it is characterized in that: described first impurity and then dehydration is at the 4th step oil phase principal product N that obtain of liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2The middle cleaner that adds first carries out adsorption-edulcoration, carries out solid-liquid behind the adsorption-edulcoration and separates, and adds dewatering agent again and dewater in the liquid phase that the solid-liquid separation obtains.
7. trimethyl fluoride sulfonyl fluorine according to claim 1 prepares N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, it is characterized in that: described removal of impurities and dehydration are carried out simultaneously, are at the 4th step oil phase principal product N that obtain of liquid-liquid separation, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Middle cleaner and the dewatering agent of adding simultaneously carries out removal of impurities and dehydration.
According to claim 5 or 6 or 7 described trimethyl fluoride sulfonyl fluorine prepare N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, it is characterized in that: described dewatering agent is Na 2SO 4, P 2O 5, in gac, diatomite or the molecular sieve any one.
According to claim 5 or 6 or 7 described trimethyl fluoride sulfonyl fluorine prepare N, N-diethyl trimethyl fluoride sulfonyl amine CF 3SO 2N (C 2H 5) 2Method, it is characterized in that: described cleaner is any one in gac, diatomite or the molecular sieve.
CN2008102436289A 2008-12-11 2008-12-11 Process for preparing N, N-diethyltrifluoromethanesulfonamide CF3SO2N (C2H5)2from trifluoromethanesulfonyl fluoride Active CN101747245B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2008102436289A CN101747245B (en) 2008-12-11 2008-12-11 Process for preparing N, N-diethyltrifluoromethanesulfonamide CF3SO2N (C2H5)2from trifluoromethanesulfonyl fluoride

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2008102436289A CN101747245B (en) 2008-12-11 2008-12-11 Process for preparing N, N-diethyltrifluoromethanesulfonamide CF3SO2N (C2H5)2from trifluoromethanesulfonyl fluoride

Publications (2)

Publication Number Publication Date
CN101747245A CN101747245A (en) 2010-06-23
CN101747245B true CN101747245B (en) 2013-01-02

Family

ID=42474931

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2008102436289A Active CN101747245B (en) 2008-12-11 2008-12-11 Process for preparing N, N-diethyltrifluoromethanesulfonamide CF3SO2N (C2H5)2from trifluoromethanesulfonyl fluoride

Country Status (1)

Country Link
CN (1) CN101747245B (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115448857A (en) * 2021-06-08 2022-12-09 联化科技（台州）有限公司 Method for continuously preparing sulfonamide compound
CN113801040A (en) * 2021-10-11 2021-12-17 石家庄圣泰化工有限公司 Synthesis method of N, N-dimethyl trifluoromethanesulfonamide
US11680041B1 (en) * 2021-12-07 2023-06-20 Ses Holdings Pte. Ltd. Processes for producing high-purity N,N-dialkyl perfluoroalkylsulfonamide
CN116154108B (en) * 2023-03-30 2024-01-23 宁德新能源科技有限公司 Secondary battery and electricity utilization device comprising same

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
roesky， herbert w.trifluormethylsulfonylstickstoff-verbindungen.《Zeitschrift fuer Naturforschung, Teil B: Anorganische Chemie, Organische 》.1970,第25卷(第3期),252-254. *

Also Published As

Publication number Publication date
CN101747245A (en) 2010-06-23

Similar Documents

Publication Publication Date Title
CN101747245B (en) Process for preparing N, N-diethyltrifluoromethanesulfonamide CF3SO2N (C2H5)2from trifluoromethanesulfonyl fluoride
CA1319368C (en) Process for the manufacture of nitric acid esters
CN106810450A (en) The apparatus and method that a kind of catalytic reaction rectification prepares dibutyl phthalate
CN113214049A (en) Method for separating isopropanol and isopropyl ether by liquid-liquid extraction-flash evaporation
CN104874196A (en) Method for processing sodium and ammonium acetate-diazonium organic compound-methanol-water mixed solution
US20170320737A1 (en) Solvothermal method for making lithium iron phosphate
CN104193634A (en) Method for separating mixed crystals of glycine and ammonium chloride
CN104577122B (en) Lithium iron phosphate solvothermal preparation device
DE60018308T2 (en) METHOD FOR PRODUCING DIAZOMETHANE
CN103318958B (en) Separation and refining method of arsenic trioxide
CN105461525B (en) The preparation of 1,3,5 3 aldehyde radical 1,3,5-trihydroxybenzene and the reuse method of preparation process trifluoroacetic acid
CN107573252B (en) Method for recycling wastewater generated in process of producing glycine by chloroacetic acid method
CN112745252B (en) H catalysis with ionic liquid as catalyst2Method for synthesizing high-added-value mercaptoacid by addition reaction of S and olefine acid
CN106496061B (en) A kind of method of acetyl spermine in extract and separate acylation reaction liquid
CN115385363A (en) Method for separating potassium fluoride and potassium chloride by using mixed alcohol reagent
CN107937009A (en) The separation method of phenolic compound in coal tar and DCL/Direct coal liquefaction product
CN104817462B (en) The production method of triisopropanolamine
CN103319383B (en) Preparation method of p-methylsulfonylbenzoic acid
CN105566171A (en) Device for preparing H-acid
CN112225636A (en) Method for separating n-hexane and acetone by ionic liquid-liquid extraction-flash evaporation
CN101747241A (en) Method for preparing trifluoromethyl sulfonic acid potassium CF3SO3K by electrochemical fluorination gas-phase product of methanesulfonyl fluoride CH3SO2F
CN106187770A (en) A kind of method of stability height iodized vegetable fatty acids ethyl ester
CN101671038A (en) Method for comprehensively utilizing solid waste in methyl carbonate production
CN103387479A (en) Method for water removal and alcohol-water mixed solution separation in alcohol method-based separation purification of arsenic trioxide
CN114933541B (en) Method for preparing 2-methylamino-5-chlorobenzophenone

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
ASS Succession or assignment of patent right

Free format text: FORMER OWNER: YANGZHOU UNIVERSITY

Effective date: 20141211

Owner name: JIANGSU GUOTAI CHAOWEI NEW MATERIAL CO., LTD.

Free format text: FORMER OWNER: GUOTAI HUARONG CHEMICAL NEW MATERIAL CO., LTD., ZHANGJIAGANG CITY

Effective date: 20141211

C41 Transfer of patent application or patent right or utility model
COR Change of bibliographic data

Free format text: CORRECT: ADDRESS; FROM: 215633 SUZHOU, JIANGSU PROVINCE TO: 215634 SUZHOU, JIANGSU PROVINCE

TR01 Transfer of patent right

Effective date of registration: 20141211

Address after: 215634, No. 4, No. two, A, building 8, Guangdong Road, Suzhou Road, Zhangjiagang Free Trade Zone, Jiangsu, China

Patentee after: JIANGSU GUOTAI SUPER POWER NEW MATERIALS CO., LTD.

Address before: 2198 room 215633, international commodity exhibition center, Zhangjiagang Free Trade Zone, Jiangsu

Patentee before: Guotai Huarong Chemical New Material Co., Ltd., Zhangjiagang City

Patentee before: Yangzhou University