Production of bio-based liquefied petroleum gas
The disclosure provides methods for the production of liquefied petroleum gas from sustainable feedstocks, including methods comprising conversion of alcohols produced by gas fermentation for the production of propane and/or butane.
1. A method of producing liquefied petroleum gas comprising:
(a) producing a dehydration feed stream comprising ethanol and isopropanol by microbial fermentation of a gaseous substrate comprising CO, CO 2 , CH 4 , or any mixture thereof, wherein the dehydration feed stream has a water content of less than 30 wt %;
(b) contacting, in a dehydration reactor, the dehydration feed stream with a dehydration catalyst to produce a first reactor effluent stream comprising ethylene and propylene;
(c) separating a propylene stream from the first reactor effluent stream and contacting the remainder in a dimerization reactor with a dimerization catalyst to produce a second reactor effluent stream comprising butene; and
(d) contacting, in a hydrogenation reactor, the separated propylene stream and the second reactor effluent stream and hydrogen with a hydrogenation catalyst to produce a product stream comprising butane and propane.
2. The method of claim 1 , wherein the dehydration reactor operates at a temperature of from 100° C. to 500° C., of from 350° C. to 450° C., or of from 375° C. to 425° C.
3. The method of claim 1 , wherein the dehydration reactor operates at a pressure of from 0.2 MPa to 2 MPa, of from 0.2 MPa to 1 MPa, or of from 0.2 MPa to 0.7 MPa.
4. The method of claim 1 , wherein the dehydration reactor operates at a whsv of from 1 h −1 to 10 h −1 , of from 2 h −1 to 8 h −1 , or of 0.5 h −1 to 2 h −1 .
5. The method of claim 1 , wherein the dehydration catalyst is selected from acidic alumina, aluminum phosphate, silica-alumina phosphate, amorphous silica-alumina, aluminosilicate, zirconia, sulfated zirconia, tungstated zirconia, tungsten carbide, molybdenum carbide, titania, sulfated carbon, phosphated carbon, phosphated silica, phosphated alumina, acidic resin, heteropolyacid, inorganic acid, and any combination thereof.
6. The method of claim 1 , wherein the dimerization reactor operates at a temperature of from 10° C. to 150° C., of from 24° C. to 135° C., of from 38° C. to 121° C., or of from 50° C. to 60° C.
7. The method of claim 1 , wherein the dimerization reactor operates at a pressure of 0.7 MPa to 6.9 MPa, of 2.4 MPa to 4.8 MPa, of 2.8 MPa to 3.4 MPa, or of 2.0 MPa to 2.7 MPa.
8. The method of claim 1 , wherein the dimerization catalyst comprises an ionic liquid catalyst.
9. The method of claim 1 , wherein the dimerization catalyst comprises a co-catalyst or a promoter.
10. The method of claim 1 , wherein the dimerization catalyst comprises a Ti(IV)/AlEt3 catalyst.
11. The method of claim 1 , wherein the hydrogenation reactor operates at a temperature of less than 400° C., of less than 250° C., or of 100° C. to 150° C.
12. The method of claim 1 , wherein the hydrogenation reactor operates at a pressure above 1.7 MPa, of 0.7 MPa to 8.2 MPa, of 0.7 MPa to 2.0 MPa, or of 1.0 MPa to 2.0 MPa.
13. The method of claim 1 , wherein the hydrogenation catalyst comprises a Ni-alumina, Pd—C, Raney-Ni, Co, or Pt catalyst, or any combination thereof.