Adiabatic plug flow reactors and processes incorporating the same
The present invention provides adiabatic plug flow reactors suitable for the production of chlorinated and/or fluorinated propene and higher alkenes from the reaction of chlorinated and/or fluorinated alkanes and chlorinated and/or fluorinated alkenes. The reactors comprise one or more designs that minimize the production of by-products at a desired conversion.
1. A process for producing a chlorinated and/or fluorinated propene, having the formula CH 2-c-g Cl c F g =CH 1-d-h Cl d F h- CH 3-e-f Cl e F f wherein c is 0-2, d is 0-1, e is 0-3, f is 0-3, g is 0-2 and h is 0-1, while c+g≤2, d+h≤1, and e+f≤3 which process comprises providing a feed comprising methanes, chloromethanes, fluoromethanes, or chlorofluoromethanes, having the formula CH 4-a-b Cl a F b , wherein each a and b are independently 0-3 and 4-a-b is greater than 0, and a chloroethylene or chlorofluoroethylene in an adiabatic plug flow reactor wherein the reactor is operably disposed relative to a mixer having a diameter and shape that are the same as those of the reactor, the reactants flow through the mixer, and the reactor further comprises a collector having the same shape and/or diameter as the reactor; wherein a turbulence flow region exists within at least a portion of the reactor having a Reynolds number (Re) of at least 2100, wherein the adiabatic plug flow reactor further comprises at least one of i) an insulation material, ii) a temperature controller for the reactor effluent; or iii) one or more temperature and flow controllers for one or more reactants, initiator(s) and/or diluents; wherein the reactor provides reduced backmixing and/or recirculation prior to entry into, or upon exit from, the reactor.
2. The process of claim 1 , wherein the reactor comprises a collector configured to accept a reactor effluent from the reactor and further configured to minimize backmixing and/or recirculation.
3. The process of claim 1 , wherein the reactor comprises a mixer configured to accept one or more reactants, initiators, and/or diluents and further configured to minimize backmixing and/or recirculation of the same.
4. The process of claim 1 , wherein the reactor inlet temperature is at least 370° C. or the reactor productivity is at least 40 gr/hr/l.
5. The process of claim 1 , wherein the reactor
i. minimizes heat transfer to and/or from the reactor;
ii. optimizes the flow of the reaction mixture at a boundary between the reaction mixture and at least a portion of at least one reactor tube wall;
iii. facilitates a reduction of the temperature of a reactor effluent to a temperature below which substantial formation of by-products does not occur, and/or
iv. allows the production rate in the reactor to be adjusted by controlling the temperature of the reactor effluent.
6. The process of claim 5 , wherein the reactor
i. minimizes heat transfer to and/or from the reactor;
ii. optimizes the flow of the reaction mixture at a boundary between the reaction mixture and at least a portion of at least one reactor tube wall;
iii. facilitates a reduction of the temperature of a reactor effluent to a temperature below which substantial formation of by-products does not occur, and
iv. allows the production rate in the reactor to be adjusted by controlling the temperature of the reactor effluent.
7. The process for preparing 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze) comprising preparing 1,1,2,3-tetrachloropropene by the process of claim 1 , and converting the 1,1,2,3-tetrachloropropene into 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze).
8. The process for preparing 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze) comprising preparing 1,1,2,3-tetrachloropropene by the process of claim 2 , and converting the 1,1,2,3-tetrachloropropene into 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze).
9. The process for preparing 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze) comprising preparing 1,1,2,3-tetrachloropropene by the process of claim 3 , and converting the 1,1,2,3-tetrachloropropene into 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze).
10. The process for preparing 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze) comprising preparing 1,1,2,3-tetrachloropropene by the process of claim 4 , and converting the 1,1,2,3-tetrachloropropene into 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze).
11. The process for preparing 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze) comprising preparing 1,1,2,3-tetrachloropropene by the process of claim 5 , and converting the 1,1,2,3-tetrachloropropene into 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze).
12. The process for preparing 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze) comprising preparing 1,1,2,3-tetrachloropropene by the process of claim 6 , and converting the 1,1,2,3-tetrachloropropene into 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) or 1,3,3,3-tetrafluoroprop-1-ene (HFO-1234ze).
13. The process of claim 2 , wherein the reactor comprises a mixer configured to accept one or more reactants, initiators, and/or diluents and further configured to minimize backmixing and/or recirculation of the same.
14. The process of claim 13 , wherein the chlorinated and/or fluorinated alkane and chlorinated and/or fluorinated alkene is selected from methanes, chloromethanes, fluoromethanes, or chlorofluoromethanes, having the formula CH 4-a-b Cl a F b , wherein each a and b are independently 0-3 and 4-a-b is greater than 0.