Abstract: We provide a process for regenerating a used acidic ionic liquid catalyst which has been deactivated by conjunct polymers in a reactor, by removing at least 57 wt % of the conjunct polymers originally present in the used acidic ionic liquid catalyst in a separate regeneration reactor, so as to increase the activity of the catalyst. We also provide a regenerated used acidic ionic liquid catalyst having increased activity.

Abstract: Processes for shutting down a regeneration reactor and for removing spent solid from the regeneration reactor may comprise shutting off a feed comprising an ionic liquid to the regeneration reactor, cooling the regeneration reactor, removing at least a portion of the ionic liquid from the regeneration reactor, purging the regeneration reactor with N2 gas, introducing water into the regeneration reactor to form an acidic liquid in the regeneration reactor, and dumping the acidic liquid and the spent solid from the regeneration reactor. The acidic liquid may be neutralized with a basic liquid to provide a neutralized liquid. The spent solid may be separated from the neutralized liquid. In an embodiment, noble metal(s) may be recovered from the spent solid.

Abstract: Processes for shutting down a regeneration reactor and for removing spent solid from the regeneration reactor may comprise shutting off a feed comprising an ionic liquid to the regeneration reactor, cooling the regeneration reactor, removing at least a portion of the ionic liquid from the regeneration reactor, purging the regeneration reactor with N2 gas, introducing water into the regeneration reactor to form an acidic liquid in the regeneration reactor, and dumping the acidic liquid and the spent solid from the regeneration reactor. The acidic liquid may be neutralized with a basic liquid to provide a neutralized liquid. The spent solid may be separated from the neutralized liquid. In an embodiment, noble metal(s) may be recovered from the spent solid.

Abstract: We provide a process for regenerating a used acidic ionic liquid catalyst which has been deactivated by conjunct polymers in a reactor, by removing at least 57 wt % of the conjunct polymers originally present in the used acidic ionic liquid catalyst in a separate regeneration reactor, so as to increase the activity of the catalyst. We also provide a regenerated used acidic ionic liquid catalyst having increased activity.

Abstract: We provide an integrated process to produce alkylate gasoline, comprising: a. alkylating a mixture of hydrocarbons using a chloride-containing ionic liquid catalyst in an alkylation reactor to produce an alkylate gasoline comprising a chloride contaminant; b. hydro-regenerating the chloride-containing ionic liquid catalyst in a hydrogenation reactor; c. hydro-dechlorinating the alkylate gasoline comprising the chloride contaminant in a dechlorination reactor at a dechlorination pressure from 0 to 1000 psig of a hydrogenation pressure used in the hydrogenation reactor, to produce a dechlorinated alkylate gasoline; and d. feeding an off-gas, comprising 70 to 99.9 vol % hydrogen, from the dechlorination reactor to the hydrogenation reactor. We also provide an integrated alkylation process unit for conducting this process.

Abstract: We provide an integrated process to produce alkylate gasoline, comprising: a. alkylating a mixture of hydrocarbons using a chloride-containing ionic liquid catalyst in an alkylation reactor to produce an alkylate gasoline comprising a chloride contaminant; b. hydro-regenerating the chloride-containing ionic liquid catalyst in a hydrogenation reactor; c. hydro-dechlorinating the alkylate gasoline comprising the chloride contaminant in a dechlorination reactor at a dechlorination pressure from 0 to 1000 psig of a hydrogenation pressure used in the hydrogenation reactor, to produce a dechlorinated alkylate gasoline; and d. feeding an off-gas, comprising 70 to 99.9 vol % hydrogen, from the dechlorination reactor to the hydrogenation reactor. We also provide an integrated alkylation process unit for conducting this process.

Abstract: We provide a process for regenerating a used acidic ionic liquid catalyst which has been deactivated by conjunct polymers in a reactor, by removing at least 57 wt % of the conjunct polymers originally present in the used acidic ionic liquid catalyst in a separate regeneration reactor, so as to increase the activity of the catalyst. We also provide a regenerated used acidic ionic liquid catalyst having increased activity.

Abstract: Olefins and alcohols present in Fischer-Tropsch products are converted to primary and secondary alkyl alcohols having at least four carbons through acid catalyzed etherification and hydrolysis reactions. The alcohols are added to a highly isoparaffinic distillate fuel blend, improving the lubricity of the mixture, and forming a distillate fuel with improved lubricity.

Abstract: Olefins and alcohols present in Fischer-Tropsch products are converted to primary and secondary alkyl alcohols having at least four carbons through acid catalyzed etherification and hydrolysis reactions. The alcohols are added to a highly isoparaffinic distillate fuel blend, improving the lubricity of the mixture, and forming a distillate fuel with improved lubricity.

Abstract: Olefins and alcohols present in Fischer-Tropsch light naphthas are converted to dialkyl ethers of the formula: R—O—R′ where R and R′ are each primarily non-tertiary alkyl groups of more than four carbon atoms, via hydration of the olefins to alcohols followed by dehydration of the alcohols. Ethers may also form by direct reaction of olefins and alcohols. The ethers are separated from the remaining paraffins in the naphtha by distillation and added in an amount of 1-25 wt. % to paraffinic mid-distillate fuel components obtained by hydrotreating a Fischer-Tropsch product. The properties of the distillate fuel components such as lubricity and seal swell are improved by the dialkyl ethers. The removal of olefins and alcohols from the naphthas reduces refining and lead to a more salable product.

Abstract: A Fischer-Tropsch C3-C4 olefin stream is simultaneously dehydrated and isomerized to convert alcohols to olefins and 1-butenes to 2-butenes and thereby lower the oxygenate content. Another Fischer-Tropsch fraction is hydrotreated and hydrocracked to provide an isobutane stream. The treated C3-C4 olefin stream having an oxygenate content less than 4000 ppm, is reacted with the isobutane stream to provide a highly branched, high octane isoparaffinic alkylate. The alkylate is useful as a blending component in motor gasoline.

Abstract: A Fischer-Tropsch C3-C4 olefin stream is treated to lower the oxygenate content to below 4000 ppm. Another Fischer-Tropsch fraction is hydrotreated and hydrocracked to provide an isobutane-containing stream. The treated C3-C4 olefin stream is reacted with the isobutane stream in an alkylation reactor to provide a highly branched, high octane isoparaffinic alkylate. The alkylate is useful as a blending component in motor gasoline.

Abstract: Olefins and alcohols present in Fischer-Tropsch light naphthas are converted to dialkyl ethers of the formula: R—O—R′ where R and R′ are each primarily non-tertiary alkyl groups of more than four carbon atoms, via hydration of the olefins to alcohols followed by dehydration of the alcohols. Ethers may also form by direct reaction of olefins and alcohols. The ethers are separated from the remaining paraffins in the naphtha by distillation and added in an amount of 1-25 wt. % to paraffinic mid-distillate fuel components obtained by hydrotreating a Fischer-Tropsch product. The properties of the distillate fuel components such as lubricity and seal swell are improved by the dialkyl ethers. The removal of olefins and alcohols from the naphthas reduces refining and lead to a more salable product.

Abstract: Olefins and alcohols present in Fischer-Tropsch products are converted to primary and secondary alkyl alcohols having at least four carbons through acid catalyzed etherification and hydrolysis reactions. The alcohols are added to a highly isoparaffinic distillate fuel blend, improving the lubricity of the mixture, and forming a distillate fuel with improved lubricity.

Abstract: A Fischer-Tropsch C3-C4 olefin stream is treated to lower the oxygenate content to below 4000 ppm. Another Fischer-Tropsch fraction is hydrotreated and hydrocracked to provide an isobutane-containing stream. The treated C3-C4 olefin stream is reacted with the isobutane stream in an alkylation reactor to provide a highly branched, high octane isoparaffinic alkylate. The alkylate is useful as a blending component in motor gasoline.

Abstract: A Fischer-Tropsch C3-C4 olefin stream is simultaneously dehydrated and isomerized to convert alcohols to olefins and 1-butenes to 2-butenes and thereby lower the oxygenate content. Another Fischer-Tropsch fraction is hydrotreated and hydrocracked to provide an isobutane stream. The treated C3-C4 olefin stream having an oxygenate content less than 4000 ppm, is reacted with the isobutane stream to provide a highly branched, high octane isoparaffinic alkylate. The alkylate is useful as a blending component in motor gasoline.