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Separation method of 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene

A technology for tetrafluoropropane and trifluoropropene is applied in the field of separation of 2-chloro-1,1,1,2-tetrafluoropropane, which can solve the problems of increasing equipment, operators and environmental hazards, and achieve a green separation process. Safe, easy to implement, and simple to operate

Active Publication Date: 2018-05-25
XIAN MODERN CHEM RES INST
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

In addition, the introduced entrainer HF is a highly corrosive medium, which increases the danger to equipment, operators and the environment

Method used

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  • Separation method of 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene
  • Separation method of 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene
  • Separation method of 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0024]Both the extractive distillation tower T1 and the extraction recovery tower T2 are packed towers with a diameter of Φ25mm and Φ3×3θ ring stainless steel packing inside, and the height of the packing layer is 4m. The rectification material 1 is the crude product of synthetic 2-chloro-1,1,1,2-tetrafluoropropane, wherein the mass percentage of HCFC-244bb is 90%, and the mass percentage of HCFO-1233xf is 10%. The material 1 is fed from the middle part of the extractive distillation tower T1, and the flow rate is 100g / h, and the bottom distillate 5 of the T2 tower (that is, the circulating extractant, N, N-dimethylformamide) is fed from the upper part of the T1 tower, The flow rate is 400g / h, T1 overhead distillate 2 is HCFC-244bb product, T1 tower still distillate 3 is HCFO-1233xf and extractant, and enters the extraction recovery tower T2 tower. T2 overhead distillate 4 is HCFO-1233xf product, and T2 tower still distillate 5 is extractant, which is returned to T1. See Tabl...

Embodiment 2

[0030] The operating process of Example 2 is similar to that of Example 1, except that the operating parameters of the rectifying towers T1 and T2 are different. The operating parameters are shown in Table 3, and the stream composition of Example 2 is shown in Table 4.

[0031] Tower operation condition in the embodiment 2 of table 3

[0032] Distillation column

T1

T2

Operating pressure / kPa(A)

200

100

Tower top temperature / ℃

34.1

12.2

Tower kettle temperature / ℃

168

152.2

Reflux ratio

5

20

[0033] The logistics composition in the embodiment 2 of table 4

[0034]

Embodiment 3

[0036] The operation process of embodiment 3 is similar to embodiment 1, and the difference is that the composition of material (1) becomes HCFC-244bb85%, HCFO-1233xf 5%, and the extractant browsing is adjusted to 1000g / h, and operating parameters are shown in Table 5, The logistics composition of embodiment 3 is shown in table 6.

[0037] Tower operation condition in the embodiment 3 of table 5

[0038] Distillation column

T1

T2

Operating pressure / kPa(A)

200

100

Tower top temperature / ℃

34.1

12.1

Tower kettle temperature / ℃

174.4

152.2

Reflux ratio

5

20

[0039] The logistics composition in the embodiment 3 of table 6

[0040]

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Abstract

The invention provides a separation method of 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene with the advantages that the operation process is green, safe and efficient. According to the method, halogenated hydrocarbon, alcohols, ether, nitrile, ketone, amide or sulphoxide with the boiling point in a range being 50 to 250 DEG C are used as extraction agents; a mixture of the 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene is separated through extraction and rectification, wherein the mass ratio of the extraction agents to the mixture of the 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene is 4:1 to 10:1.

Description

technical field [0001] The present invention relates to a method for separating 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene, in particular to extractive distillation from 2-chloro-1 , A method for separating 2-chloro-1,1,1,2-tetrafluoropropane from a mixture of 1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene. Background technique [0002] 2-Chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb) is the raw material for the synthesis of 2,3,3,3-tetrafluoropropene (HFO-1234yf). HFO-1234yf, with zero ozone depletion potential and 4 greenhouse effect potential, has excellent environmental performance and is considered as an ideal substitute for 1,1,1,2-tetrafluoroethane (HFC-134a). [0003] 2-Chloro-1,1,1,2-tetrafluoropropane is mainly produced by the liquid-phase fluorination reaction of hydrogen fluoride and 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), which is affected by the catalyst and the reaction itself Influenced by characteristics, t...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C19/10C07C17/386
CPCC07C17/386C07C19/10
Inventor 吕剑曾纪珺韩升唐晓博张伟郝志军杨志强李晨亢建平王博李凤仙
Owner XIAN MODERN CHEM RES INST