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Method for purifying 1,1,1,2-tetrafluoroethane through purification reaction

A purification method and technology of tetrafluoroethane, applied in chemical instruments and methods, organic chemistry, preparation of halogenated hydrocarbons, etc., can solve uneconomical problems and achieve the effect of solving difficult-to-control and accelerating the transfer of reaction heat

Inactive Publication Date: 2018-10-09
JIANGSU SANMEI CHEM
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0008] Molecular sieve adsorption method (CN 1069259, US4906796, EP511612, JP03072437), this method is an industrial method for removing trace olefin impurities from crude hydrofluorocarbon products, many patents have reported, but it can only be used for final treatment in industry , when the adsorbed impurity content is greater than tens of ppm, it is very uneconomical

Method used

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  • Method for purifying 1,1,1,2-tetrafluoroethane through purification reaction
  • Method for purifying 1,1,1,2-tetrafluoroethane through purification reaction
  • Method for purifying 1,1,1,2-tetrafluoroethane through purification reaction

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Effect test

Embodiment 1

[0025] Trichlorethylene and anhydrous hydrogen fluoride enter the second reactor 2 together, and carry out the second-step reaction at a higher temperature of 350 ° C, and the gas product from the second reactor 2 enters the first reactor together with supplemented trichlorethylene 1. After the first step of the reaction is completed to generate HCFC-133a mixture, the reaction mixture enters the purification reactor 6, and the temperature of the purification reaction is controlled at 180°C.

[0026] The mixed gas entering the purification reactor 6 is: the molar ratio of HF / R134a is 0.25, the R1122 content in the mixed gas is 1500ppm, other olefins are 80ppm, and the hydrogen chloride content is 43% (by mass). The mixed gas is passed into the purification reactor, the reaction pressure is 1.2MPa, and the residence time (t) of the mixed gas is set at 70s.

[0027] The material after the purification reaction was tested, and the content of R1122 was 1456ppm, and the total conten...

Embodiment 2

[0029] The material undergoes the second step reaction at a higher temperature of 350°C, and the gas product from the second reactor 2 enters the first reactor 1 together with supplemented trichlorethylene, and the first step reaction is completed to generate HCFC-133a The mixture, the reaction mixture enters the HCl separation tower 3, HCl is removed first, and then the HFC-134a crude product is obtained by separation through the crude product tower 4, and the unreacted HF, HCFC-133a and supplemented HF are sent into the second reactor 2 together, and the remaining gas enters The purification reactor 6 reacts, and the HFC-134a enters the purification device 7 for purification after being catalyzed by the purification reactor 6 to purify and remove olefins by fluorination.

[0030] The mixed gas entering the purification reactor 6 is: the molar ratio of HF / R134a is 0.25, the content of R1122 in the mixed gas is 1500ppm, the content of other olefins is 80ppm, and the content of ...

Embodiment 3

[0035]The material undergoes the second step reaction at a higher temperature of 350°C, and the gas product from the second reactor 2 enters the first reactor 1 together with supplemented trichlorethylene, and the first step reaction is completed to generate HCFC-133a, and the reaction The mixture enters the HCl separation tower 3, HCl is removed first, and then the crude product of HFC-134a is separated by the crude product tower 4, and the unreacted HF, HCFC-133a and supplemented HF are sent to the second reactor 2 together, and the remaining gas enters the purification reactor 6 reaction, HFC-134a enters the purification device 7 for purification after the purification reactor 6 catalyzes the fluorination purification and olefin removal reaction.

[0036] The mixed gas entering the purification reactor 6 is: the molar ratio of HF / R134a is 0.25, the content of R1122 in the mixed gas is 1500ppm, the content of other olefins is 80ppm, and the content of hydrogen chloride is 10p...

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Abstract

The invention discloses a method for purifying 1,1,1,2-tetrafluoroethane through purification reaction. The reaction is carried out through a reverse cycle and the method comprises the following steps: carrying out two-step catalytic fluorination reaction by adopting two reactors respectively; taking trichloroethylene and anhydrous hydrogen fluoride as raw materials and conveying into a second reactor; carrying out second-step reaction under relatively high temperature; conveying a gas product produced by the second reactor and supplemented trichloroethylene into a first reactor; carrying outfirst-step reaction to generate an HCFC-133a mixture; conveying the HCFC-133a mixture into an HCl separation tower; firstly, removing HCl and then separating to obtain an HFC-134a crude product.

Description

technical field [0001] The present invention relates to a preparation method of 1,1,1,2-tetrafluoroethane, in particular to a method for removing one or more compounds contained in 1,1,1,2-tetrafluoroethane through gas phase fluorination reaction. Method for Unsaturated Hydrocarbon Impurities. Background technique [0002] In recent years, the destruction of the ozone layer by CFCs has become increasingly serious, and 1,1,1,2-tetrafluoroethane (HFC-134a) is a colorless, non-toxic, non-combustible chemical substance, and is a HFC-type refrigeration agent, the Ozone Depletion Potential (ODP) value is zero. The thermodynamic performance of HFC-134a is very similar to that of CFC-12, and its safety is comparable to that of CFC-12. It has been recognized as the best substitute of CFC-12. [0003] At present, the ideal industrial production of HFC-134a is: catalytic fluorination with trichlorethylene and anhydrous hydrogen fluoride in a gas phase environment. A known feature of...

Claims

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Application Information

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IPC IPC(8): C07C19/08C07C17/20C07C17/395C07C17/087C07C19/12C07C21/18
CPCC07C17/087C07C17/206C07C17/395C07C21/18C07C19/12C07C19/08
Inventor 徐志雄童绍丰丛鑫鑫张伟徐科
Owner JIANGSU SANMEI CHEM
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