초록 ▼

This invention relates to a method of making an olefin from a dialkyl ether comprising (a) introducing an ether having a formula CxH2x+1CyH2y+1 into a thermal or catalytic cracking unit processing a hydrocarbon feedstock; and (b) decomposing at least a portion of the ether to form an olefin having a

This invention relates to a method of making an olefin from a dialkyl ether comprising (a) introducing an ether having a formula CxH2x+1CyH2y+1 into a thermal or catalytic cracking unit processing a hydrocarbon feedstock; and (b) decomposing at least a portion of the ether to form an olefin having a formula CxH2x and/or CyH2y and an alcohol having a formula CxH2x+1 and/or CyH2y+1OH, wherein x and y independently range from about 1 to about 30. This invention also relates to a method of reducing coking in a thermal or catalytic cracking unit comprising (a) introducing an ether, having a formula CxH2x+1OCyH2y+1, into the cracking unit processing a hydrocarbon feedstock in an amount effective to reduce coke formation relative to processing the hydrocarbon feedstock in the absence of the ether, wherein x and y independently range from about 1 to about 30.

대표청구항 ▼

The invention claimed is: 1. A method of making an olefin from a dialkyl ether, the method comprising: (a) independently introducing an ether having a formula CxH2x+1 OCyH2y+1 into a thermal or catalytic cracking unit selected from the group consisting of a FCC, a delayed coker, a fluid coker, or a

The invention claimed is: 1. A method of making an olefin from a dialkyl ether, the method comprising: (a) independently introducing an ether having a formula CxH2x+1 OCyH2y+1 into a thermal or catalytic cracking unit selected from the group consisting of a FCC, a delayed coker, a fluid coker, or a steam cracking unit, said thermal or catalytic unit processing a hydrocarbon feedstock selected from the group consisting of crude oils, naphtha, vacuum gas oils, thermal oils, residual oils, cycle stocks, topped whole crudes, tar sand oil, shale oils, synthetic fuels, heavy hydrocarbon fractions derived from the destructive hydrogenation of coal, tar, pitches, asphalts, a gas-to-olefins derived feedstock, hydrotreated feedstocks derived therefrom, and mixtures thereof; and (b) decomposing at least a portion of said ether to form (1) an olefin having a formula CyH2x and/or CyH2y and (2) an alcohol having a formula CxH2x+1OH and/ or CyH2y+1OH; (c) recovering at least a portion of the alcohol; (d) introducing at least a portion of the alcohol into the thermal or catalytic cracking unit; (e) decomposing at least a portion of the alcohol to form the olefin; wherein the ether comprises from at least about 1 weight % to about 5 weight % of the total weight of the feedstock and the ether; wherein x and y independently range from about 1 to 10; and whereby said ether reduces coke formation relative to processing said hydrocarbon feedstock in the absence of said ether. 2. The method according to claim 1, wherein a liquefied petroleum gas yield ranges from about 10 weight % to about 82 weight %. 3. The method according to claim 2, wherein the liquefied petroleum gas comprises C3 and C4 olefins ranging from about 35 weight % to about 91 weight % of the total weight of the liquefied petroleum gas. 4. The method according to claim 1, wherein x and y independently range from about 1 to 10. 5. The method according to claim 1, wherein the ether and the alcohol are each independently introduced at one or more points in the thermal or catalytic cracking unit selected from (a) the feedstock feedline prior to addition of a dispersion steam stream, (b) a bottom section of the riser downstream of the hydrocarbon feed steam mixer and the regenerated catalyst return line, (c) a bottom section of a stripper, (d) a middle section of the stripper, (e) the top section of the stripper, (f) in a vapor line exiting the stripper, or (g) a fractionator. 6. The method according to claim 1, wherein the thermal or catalytic cracking unit comprises a stripper bed operating at a temperature ranging from at least about 480° C. to about 650° C.