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

A technology of tetrafluoropropene and its production method, which is applied in the production field of 2,3,3,3-tetrafluoropropene, can solve the problems of easy coking and deactivation of the catalyst, short service life, short continuous production cycle, etc., and achieve the extension of continuous production cycle, the effect of inhibiting coking

Active Publication Date: 2010-12-15
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 th

Method used

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

Examples

Experimental program
Comparison scheme
Effect test

Example Embodiment

[0036] Example 1

[0037] The thermal cracking reactor 4 in this embodiment adopts an externally heated reactor with a tube diameter of ∮19×2 mm, and the diluent gas is nitrogen. The process flow is:

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

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

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

[0041] D. The pyrolysis reaction product is quenched to 50°C through the quenching device;

[0042] E. Post-processing

[0043] E-a. Acid removal: The product obtained in step D enters the water alkaline washing and acid re...

Example Embodiment

[0048] Example 2

[0049] The thermal cracking reactor 4 in this embodiment adopts an externally heated reactor with a pipe diameter of ∮19×2 mm, and the diluent gas is steam. The process flow is:

[0050] A. Preheat water vapor to 1100°C through the diluent gas preheating device 1; meanwhile, preheat HCFC-244bb to 300°C through the HCFC-244bb preheating device 2;

[0051] B. After preheating, water vapor and HCFC-244bb enter the material mixing device 3, and they are mixed according to the molar ratio of water vapor and HCFC-244bb of 5:1;

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

[0053] D. The pyrolysis reaction product is heated to 150°C through the quenching treatment device;

[0054] E. Post-processing

[0055] E-a, dehydration, deacidification: the product obtaine...

Example Embodiment

[0059] Example 3

[0060] The thermal cracking reactor 4 in this embodiment adopts an externally heated reactor with a tube diameter of ∮19×2 mm, and the diluent gas is HF. The process flow is:

[0061] A. Preheat HF ​​to 900°C through the diluent gas preheating device 1; meanwhile preheat HCFC-244bb to 300°C through the HCFC-244bb preheating device 2;

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

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

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

[0065] E. Post-processing

[0066] Ea. Separation and deacidification: First, the product obtained in step D is separated through separation 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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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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