A process for upgrading resid, comprising: hydrocracking a resid in a first reaction stage to form a first stage effluent; hydrocracking a deasphalted oil fraction in a second reaction stage to form a second stage effluent; feeding the first stage effluent and the second stage effluent to a separation system; fractionating the first stage effluent and the second stage effluent in the separation system to recover at least one distillate hydrocarbon fraction and a resid hydrocarbon fraction; and feeding the resid hydrocarbon fraction to a solvent deasphalting unit to provide an asphaltene fraction and the deasphalted oil fraction, wherein hydrocracking a resid comprises: feeding hydrogen and the resid to a first reactor containing a first hydrocracking catalyst; contacting the resid and hydrogen in the presence of the first hydrocracking catalyst at conditions of temperature and pressure to crack at least a portion of the resid; recovering the first stage effluent from the first reactor; wherein hydrocracking a deasphalted oil fraction comprises: feeding hydrogen and the deasphalted oil fraction to a second reactor containing a second hydrocracking catalyst; contacting the deasphalted oil fraction and hydrogen in the presence of the second hydrocracking catalyst at conditions of temperature and pressure to crack at least a portion of the deasphalted oil; and recovering the second stage effluent from the second reactor, and wherein the fractionating comprises: separating the first and second stage effluents in a high pressure high temperature separator to provide a gas phase product and a liquid phase product; separating the liquid phase product in an atmospheric distillation tower to recover a fraction comprising hydrocarbons boiling in a range of atmospheric distillates and a first bottoms fraction comprising hydrocarbons having a normal boiling point of at least 340°C; separating the bottoms fraction in a vacuum distillation tower to recover a fraction comprising hydrocarbons boiling in a range of vacuum distillates and a second bottoms fraction comprising hydrocarbons having a boiling temperature of at least 480°C; and feeding the second bottoms fraction to the solvent deasphalting unit as the resid hydrocarbon fraction. hydrocracking a resid in a first reaction stage to form a first stage effluent; hydrocracking a deasphalted oil fraction in a second reaction stage to form a second stage effluent; feeding the first stage effluent and the second stage effluent to a separation system; fractionating the first stage effluent and the second stage effluent in the separation system to recover at least one distillate hydrocarbon fraction and a resid hydrocarbon fraction; and feeding the resid hydrocarbon fraction to a solvent deasphalting unit to provide an asphaltene fraction and the deasphalted oil fraction, feeding hydrogen and the resid to a first reactor containing a first hydrocracking catalyst; contacting the resid and hydrogen in the presence of the first hydrocracking catalyst at conditions of temperature and pressure to crack at least a portion of the resid; recovering the first stage effluent from the first reactor; feeding hydrogen and the deasphalted oil fraction to a second reactor containing a second hydrocracking catalyst; contacting the deasphalted oil fraction and hydrogen in the presence of the second hydrocracking catalyst at conditions of temperature and pressure to crack at least a portion of the deasphalted oil; and recovering the second stage effluent from the second reactor, and separating the first and second stage effluents in a high pressure high temperature separator to provide a gas phase product and a liquid phase product; separating the liquid phase product in an atmospheric distillation tower to recover a fraction comprising hydrocarbons boiling in a range of atmospheric distillates and a first bottoms fraction comprising hydrocarbons having a normal boiling point of at least 340°C; separating the bottoms fraction in a vacuum distillation tower to recover a fraction comprising hydrocarbons boiling in a range of vacuum distillates and a second bottoms fraction comprising hydrocarbons having a boiling temperature of at least 480°C; and feeding the second bottoms fraction to the solvent deasphalting unit as the resid hydrocarbon fraction.