Simultaneous dehydration, dimerization, and metathesis of C2-C5 alcohols
This disclosure relates to a single stage process for the direct conversion of alcohols, e.g. ethanol, to olefinic mixtures (C 2 -C 7 ) with low levels of aromatics carried out in a single reactor with two fixed catalyst beds in series, or two catalytic fixed bed reactors in series wherein the first reactor operates at a lower or higher temperature than the operating temperature of the second reactor. The process transformation of ethanol is comprised of ethanol dehydration to ethylene and water in high yield with the first catalyst in the first reactor, or via the first fixed catalyst bed, followed by directly feeding the ethylene and water to the second reactor, or second fixed catalyst bed, with conversion of said ethylene and water to a C 2 -C 7 olefinic mixture with the second catalyst(s) in high yields with minimal aromatic compound formation.
1 . A process for converting one or more C2-C5 linear or branched alcohols to one or more C2-C7 olefins, the process comprising:
contacting a first stream comprising the C2-C5 linear or branched alcohols with a first catalyst in a reactor at a temperature from about 200° C. to about 500° C., gauge pressure from 0 to about 30 bar, and a weight hourly space velocity (WHSV) of at least 0.5 to form a second stream; and
contacting the second stream with a second catalyst in the reactor or in a different reactor operating at a temperature from about 200° C. to about 500° C., gauge pressure from 0 to about 30 bar, and a weight hourly space velocity (WHSV) of at least 0.5, wherein the second catalyst comprises a doped zeolite catalyst that includes boron and phosphorus, thereby forming the one or more C2-C7 olefins.
2 . The process of claim 1 , wherein the first catalyst comprises an alumina catalyst.
3 . The process of claim 2 , wherein the alumina catalyst comprises a y-alumina catalyst.
4 . The process of claim 1 , wherein the one or more C2-C5 linear or branched alcohols is ethanol, propanol, butanol, or any combination thereof.
5 . The process of claim 1 , wherein the one or more C2-C5 linear or branched alcohols are bio-based and produced by fermentative processes.
6 . The process of claim 1 , wherein the one or more C2-C5 linear or branched alcohols are not derived from petroleum.
7 . The process of claim 1 , wherein the one or more C2-C7 olefins includes ethylene, propylene, butenes, C5-C6 olefins, one or more C2-C6 olefins, or any combination thereof.
8 . The process of claim 1 , wherein the boron and the phosphorus are each present in an amount of less than 5 wt. % of the second catalyst.
9 . The process of claim 1 , wherein the boron and the phosphorus are each present in an amount from 2 wt. % to 5 wt. % of the second catalyst.
10 . The process of claim 1 , wherein the doped zeolite catalyst comprises a ZSM-5 zeolite.
11 . The process of claim 1 , further comprising removing a portion of water from the second stream.
12 . A process for converting one or more C2-C5 linear or branched alcohols to one or more C2-C7 olefins, the process comprising:
contacting a stream comprising the C2-C5 linear or branched alcohols with at least two catalysts in a reactor at a temperature from about 200° C. to about 500° C., gauge pressure from 0 to about 30 bar, and a weight hourly space velocity (WHSV) of at least 0.5 to form the one or more C2-C7 olefins, wherein one catalyst of the at least two catalysts comprises a doped zeolite catalyst that includes boron and phosphorus, and another catalyst of the at least two catalysts is different than the one catalyst.
13 . The process of claim 12 , wherein the first catalyst comprises an alumina catalyst.
14 . The process of claim 13 , wherein the alumina catalyst comprises a γ-alumina catalyst.
15 . The process of claim 12 , wherein the boron and the phosphorus are each present in an amount of less than 5 wt. % of the second catalyst.
16 . The process of claim 12 , wherein the boron and the phosphorus are each present in an amount from 2 wt. % to 5 wt. % of the second catalyst.
17 . The process of claim 12 , wherein the doped zeolite catalyst comprises a ZSM-5 zeolite.
18 . The process of claim 12 , wherein the temperature of the reactor is from 300 ° ° C.C. to 420 ° C., from 350° C. to 450° C., from 300° C. to 450° C., or from 300° C. to 500° C.
19 . The process of claim 12 , wherein the gauge pressure of the reactor is from 0 to 10 bar or from 0 to 1 bar.
20 . The process of claim 12 , wherein the mass yield of the one or more C2-C7 olefins is from 65% to 98% or from 75% to 95%.
21 . A process for converting one or more C 2 -C 7 olefins to one or more fuels, the process comprising:
oligomerizing the one or more C2-C7 olefins of claim 12 to produce one or more fuels.
22 . The process of claim 21 , wherein the one or more fuels comprise gasoline, jet fuel, or diesel fuel.
23 . The process of claim 21 , wherein oligomerizing the one or more C2-C7 olefins of claim 21 to produce one or more fuels comprises oligomerizing the one or more C2-C7 olefins to produce hydrocarbons.
24 . The process of claim 1 , wherein the temperature of the reactor is from 300° C. to 420° C., from 350° C. to 450° C., from 300° C. to 450° C., or from 300° C. to 500° C.
25 . The process of claim 1 , wherein the gauge pressure of the reactor is from 0 to 10 bar or from 0 to 1 bar.
26 . The process of claim 1 , wherein the mass yield of the one or more C2-C7 olefins is from 65% to 98% or from 75% to 95%.
27 . A process for converting one or more C2-C7 olefins to one or more fuels, the process comprising:
oligomerizing the one or more C2-C7 olefins of claim 1 to produce one or more fuels.
28 . The process of claim 27 , wherein the one or more fuels comprise gasoline, jet fuel, or diesel fuel.
29 . The process of claim 27 , wherein oligomerizing the one or more C2-C7 olefins of claim 27 to produce one or more fuels comprises oligomerizing the one or more C2-C7 olefins to produce hydrocarbons.