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Production method of 2,3,3,3-tetrafluoropropene

A tetrafluoropropene and production method technology, applied in the production field of 2,3,3,3-tetrafluoropropene, can solve the problems of short life, easy coking and deactivation of the catalyst, short continuous production cycle, etc., and achieve coking suppression, The effect of extending the continuous production cycle

Active Publication Date: 2013-06-05
山东华安近代环保科技有限公司
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Since the catalyst is a solid acid catalyst and the target product is olefin, the catalyst is easily coked and deactivated during the reaction, and its life is short. The catalyst needs to be regenerated frequently, resulting in a short continuous production cycle.

Method used

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  • Production method of 2,3,3,3-tetrafluoropropene
  • Production method of 2,3,3,3-tetrafluoropropene

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Experimental program
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Effect test

Embodiment 1

[0037] In this embodiment, the pyrolysis reactor 4 adopts an external heating reactor with a pipe diameter of ∮19×2mm, and the diluent gas is nitrogen. Its technological process is:

[0038] A. Preheat the nitrogen to 600°C through the dilution gas preheating device 1; at the same time, preheat the HCFC-244bb to 200°C through the HCFC-244bb preheating device 2;

[0039] B, after preheating, nitrogen and HCFC-244bb enter material mixing device 3, and mix according to the mol ratio of nitrogen and HCFC-244bb as 20: 1;

[0040] C, the mixture of nitrogen and HCFC-244bb obtained in step B enters the tubular thermal cracking reactor 4, and performs thermal cracking reaction at a reaction temperature of 450 ° C and a residence time of 60 seconds;

[0041] D. The cracking reaction product is cooled to 50°C through the quenching treatment device;

[0042] E. Post-processing

[0043] E-a, acid removal: the product obtained in step D enters the water alkali washing and acid removal d...

Embodiment 2

[0049] In this embodiment, the pyrolysis reactor 4 adopts an external heating reactor with a pipe diameter of ∮19×2 mm, and the diluent gas is water vapor. Its technological process is:

[0050] A. The water vapor is preheated to 1100°C through the dilution gas preheating device 1; at the same time, the HCFC-244bb is preheated to 300°C through the HCFC-244bb preheating device 2;

[0051] B, steam and HCFC-244bb after preheating enter material mixing device 3, mix according to the mol ratio of steam and HCFC-244bb be 5: 1;

[0052] C. The mixture of water vapor and HCFC-244bb obtained in step B enters the tubular thermal cracking reactor 4, and performs thermal cracking reaction at a reaction temperature of 900°C and a residence time of 0.01 seconds;

[0053] D. The pyrolysis reaction product is cooled to 150°C by the quenching device;

[0054] E. Post-processing

[0055] E-a, dehydration, acid removal: the product obtained in step D is dehydrated by low-pressure condensation ...

Embodiment 3

[0060] Present embodiment pyrolysis reactor 4 adopts pipe diameter to be the external heating reactor of ∮ 19 * 2mm, and diluent gas is HF. Its technological process is:

[0061] A. Preheat HF ​​to 900°C through dilution gas preheating device 1; at the same time, preheat HCFC-244bb to 300°C through HCFC-244bb preheating device 2;

[0062] B, after preheating, HF and HCFC-244bb enter material mixing device 3, and mix according to the molar ratio of HF and HCFC-244bb is 1: 1;

[0063] C. The mixture of HF and HCFC-244bb obtained in step B enters the tubular thermal cracking reactor 4, and performs thermal cracking reaction at a reaction temperature of 600°C and a residence time of 0.5 seconds;

[0064] D. The cracking reaction product is cooled to 100°C through the quenching treatment device;

[0065] E. Post-processing

[0066] E-a. Separation and acid removal: first, the product obtained in step D is separated through the separation tower 6-6, and the overhead fraction of t...

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Abstract

The invention provides a production method of 2,3,3,3-tetrafluoropropene, in which 2-chloro-2,3,3,3-tetrafluoropropane is taken as a raw material for thermal cracking in the presence of diluents such as nitrogen, water vapour or HF (Hydrogen Fluoride) to prepare the 2,3,3,3-tetrafluoropropene. The method comprises the steps of: heating the diluents and preheating HCFC-244bb; mxing the diluents and the HCFC-244bb according to the mole ratio of 1-20 to 1; performing thermal cracking reaction at the reaction temperature of 450 to 900 DEG C and under the contact time of 0.01 to 60 seconds; and quenching, separating, disacidifying and rectificating to obtain the 2,3,3,3-tetrafluoropropene product. The preparation method provided by the invention needs no catalyst in the reaction process, thereby overcoming the defects that the catalyst in the prior art is easy to coke and inactivated and the continuous production period is short.

Description

technical field [0001] The present invention relates to a kind of production method of 2,3,3,3-tetrafluoropropene (HFO-1234yf), especially a kind of 2-chloro-2,3,3,3-tetrafluoropropane (HCFC-244bb) thermal Cracking to obtain 2,3,3,3-tetrafluoropropene production method. Background technique [0002] 2,3,3,3-Tetrafluoropropene has zero ozone depletion potential and low greenhouse effect gas, so it is considered as an ideal substitute for HFC-134a. US Patent US20090043136 discloses a preparation method of HFO-1234yf, which uses HCFC-244bb as a raw material, and synthesizes HFO-1234yf by removing HCl at 200°C-600°C under the action of a catalyst. Since the catalyst is a solid acid catalyst and the target product is olefin, the catalyst is easily coked and deactivated during the reaction process, and its lifespan is short. The catalyst needs to be regenerated frequently, resulting in a short continuous production cycle. Contents of the invention [0003] The purpose of the p...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C21/18C07C17/25
Inventor 吕剑张伟寇联岗曾纪珺杨志强何飞王博马洋博
Owner 山东华安近代环保科技有限公司
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