Continuous low-temperature process to produce trans-1-chloro-3,3,3-trifluoropropene
View Patent ↗Disclosed is process for the production of (E) 1-chloro-3,3,3-trifluoropropene (HCFO-1233zd(E)) by conducting a continuous reaction without the use of a catalyst. Also disclosed is an integrated system for producing hydrofluoro olefins, particularly 1233zd(E). The manufacturing process includes six major unit operations: (1) a fluorination reaction of HCC-240fa (in continuous or semi-batch mode) using HF with simultaneous removal of by-product HCl and the product 1233zd(E); (2) recycle of unreacted HCC-240fa and HF together with under-fluorinated by-products back to (1); (3) separation and purification of by-product HCl; (4) separation of excess HF back to (1); (5) purification of final product, 1233zd(E); and (6) isomerization of by-product 1233zd(Z) to 1233zd(E) to maximize the process yield.
1. An integrated system for producing (E)1-chloro-3,3,3-trifluoropropene, wherein the system comprises:
(a) one or more feed streams cumulatively comprising hydrogen fluoride and a reactant composition selected from the group consisting of 1,1,1,3,3-pentachloro-propane, or 1,1,1,3,3-pentachloropropane, and/or 1,1,3,3-tetrachloropropene, and/or 1,3,3,3-tetrachloropropene;
(b) a liquid phase reactor system consisting of a series of one or more agitated reactors, each fed by its predecessor, and wherein the liquid phase reactor series is fluidly connected to the one or more feed streams;
(c) recycle system comprising a recycle distillation column, a reflux stream fluidly connected to the top of the reactor and a combined first crude product stream fluidly connected to the top of the reactor, wherein the reflux stream is fluidly connected to a liquid phase reactor in the series;
(d) a hydrogen chloride removal system comprising a first distillation column, a hydrogen chloride by-product stream fluidly connected to the first distillation column, and a second crude product stream fluidly connected to the first distillation column, wherein the first distillation column is fluidly connected to a stripping column;
(e) a hydrogen fluoride recovery system comprising a sulfuric acid absorption and recycle system or a phase separation vessel, a second recycle stream comprising hydrogen fluoride fluidly connected to the sulfuric acid absorption and recycle system or a phase separation vessel;
(f) a third product stream comprising (E) and (Z) 1-chloro-3,3,3-trifluoro-propene fluidly connected to the sulfuric acid absorption and recycle system or a phase separation vessel, wherein the sulfuric acid absorption and recycle system or a phase separation vessel is fluidly connected to the second crude product stream and a 1-chloro-3,3,3-trifluoropropene purification system comprising a second distillation column fluidly connected to the third product stream and
(g) a final product stream comprising at least 50 wt. percent (E)1-chloro-3,3,3-trifluoropropene fluidly connected to the second distillation column; a second by-product stream fluidly connected to the distillation column, an isomerization reactor fluidly connected to the second by-product stream; and a product recycle stream fluidly connected to the isomerization reactor and the second distillation column.
2. The integrated system of claim 1 , wherein one or more of the reactors in part (b) is combined with an attached rectifying column supplied with low-temperature cooling, and maintained at a temperature of about 65° C. to about 175° C.
3. The integrated system of claim 1 , wherein the separating and recycling of HF is accomplished by phase separation.
4. The integrated system of claim 1 , wherein each reactor is maintained at a temperature range of 65° C. to 175° C.
5. The integrated system of claim 1 , wherein each reactor is maintained at a temperature range of 85° C. to 170° C.
6. The integrated system of claim 1 , wherein each reactor is maintained at a temperature range of 95° C. to 160° C.