TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: The hydrocarbon stream comprises at least one olefin from a FC cracker. The halide containing additive is present during the reacting, at a level that provides increased yield of the middle distillate. The yield of the broad boiling alkylate product exceeds the amount of olefin in the hydrocarbon stream by at least 30 wt.%. The process involves adjusting a level of a halide containing additive provided to an ionic liquid alkylation reactor to shift selectivity towards heavier products in an alkylate product; and recovering from the alkylate product the gasoline blending component that is a low volatility gasoline blending component; and the middle distillate. The middle distillate is from 29-50 wt.% of the total alkylate product. The adjusting is a lowering of the level of the halide. The yield of the alkylate product exceeds the amount of olefin supplied to the ionic liquid alkylation reactor by at least 30 wt.%. The middle distillate has a nuclear magnetic resonance branching index greater than 60. The middle distillate has a CH3/CH2 hydrogen ratio greater than 2.6. The process involves reacting an isobutane stream with a process stream containing butene under alkylation conditions where the isobutane and butene are alkylated to produce an alkylate product in the presence of a chloroaluminate ionic liquid of formula RR'R''NH+ Al2Cl7- or compound formula (I) and (II); and separating out the middle distillate and the gasoline blending component from the alkylate product; where the separated middle distillate fraction is from 20 wt% or higher of the total alkylate product; and where the separated gasoline blending component has a RON of 91 or higher. The separated middle distillate is from 29-80 wt.% of the total alkylate product. The reacting step additionally includes adjusting a level of a halide containing additive provided to an ionic liquid reactor where the reacting occurs, where the halide containing additive is unsupported. The alkylate product has less than 5 wt.% olefins prior to optional further processing.RR' and R''=1-12C alkyl;R=H, methyl, ethyl, propyl, butyl, pentyl or hexyl group;R'=H, methyl, ethyl, propyl, butyl, pentyl or hexyl group;X=chloroaluminate;R1 and R2=H, methyl, ethyl, propyl, butyl, pentyl or hexyl group. EXAMPLE - The feedstock for the alkylation was mixed C4 olefins (butene) from an FC cracker containing 40-50% olefins and the balance being isobutane and n-butane, and refinery isobutane containing greater than or equal to 80% of isobutane. The molar ratio of isoparaffin to olefin was in the range of 10:1. None of the feed to the alkylation reactor was oligomerized olefins. N-butylpyridinium chloroaluminate (C5H5NC4H9Al2Cl7) ionic liquid doped with hydrochloric acid was used as catalyst and added in a continuous stream to the alkylation reactor at a volumetric flow of 0.8 ml/minutes. The ionic liquid and the hydrochloric acid were unsupported. The level of hydrochloric acid was selected, and adjusted over time to provide a good yield of middle distillate.