A method for producing a naphtha product and an unconverted product, comprising: exposing, in a first hydrocracking stage, a first feedstock to a first hydrocracking catalyst in a first reaction vessel under first hydrocracking conditions to form a first hydrocracked effluent including at least a first liquid phase portion, at least 60 wt% of the first feedstock boiling above 204°C (400°F) and at least 60 wt% of the first feedstock boiling below 343°C (650°F), the first hydrocracking catalyst comprising Ni, Mo, and W on an acidic support, the molar ratio of Mo to W being from 2:1 to 1:2, wherein the first reaction vessel further contains a dewaxing catalyst which comprises ZSM-48, ZSM-23, zeolite Beta, or a combination thereof; fractionating the first liquid phase portion and at least a portion of a second liquid phase portion to form a first naphtha fraction and a first unconverted fraction, the first naphtha fraction corresponding to at least 80 wt% of the first feedstock and having a final boiling point of 204°C (400°F) or less; withdrawing a portion of the first unconverted fraction as a first unconverted product, a weight of the withdrawn first unconverted product corresponding to from 5 wt% to 15 wt% of the first feedstock, the withdrawn first unconverted product having an initial boiling point of at least 204°C (400°F); separating at least a portion of the remaining portion of the first unconverted fraction as a second feedstock; exposing, in a second hydrocracking stage, the second feedstock to a second hydrocracking catalyst in a second reactor vessel under second hydrocracking conditions to form a second hydrocracked effluent including at least the second liquid phase portion; and separating the second hydrocracked effluent to produce the second liquid phase portion; wherein the temperature of the second hydrocracking conditions is at least 11°C (20°F) less than the temperature of the first hydrocracking conditions, and wherein the temperature of the first hydrocracking conditions at start-of-run is less than 377°C (710°F). exposing, in a first hydrocracking stage, a first feedstock to a first hydrocracking catalyst in a first reaction vessel under first hydrocracking conditions to form a first hydrocracked effluent including at least a first liquid phase portion, at least 60 wt% of the first feedstock boiling above 204°C (400°F) and at least 60 wt% of the first feedstock boiling below 343°C (650°F), the first hydrocracking catalyst comprising Ni, Mo, and W on an acidic support, the molar ratio of Mo to W being from 2:1 to 1:2, wherein the first reaction vessel further contains a dewaxing catalyst which comprises ZSM-48, ZSM-23, zeolite Beta, or a combination thereof; fractionating the first liquid phase portion and at least a portion of a second liquid phase portion to form a first naphtha fraction and a first unconverted fraction, the first naphtha fraction corresponding to at least 80 wt% of the first feedstock and having a final boiling point of 204°C (400°F) or less; withdrawing a portion of the first unconverted fraction as a first unconverted product, a weight of the withdrawn first unconverted product corresponding to from 5 wt% to 15 wt% of the first feedstock, the withdrawn first unconverted product having an initial boiling point of at least 204°C (400°F); separating at least a portion of the remaining portion of the first unconverted fraction as a second feedstock; exposing, in a second hydrocracking stage, the second feedstock to a second hydrocracking catalyst in a second reactor vessel under second hydrocracking conditions to form a second hydrocracked effluent including at least the second liquid phase portion; and separating the second hydrocracked effluent to produce the second liquid phase portion; wherein the temperature of the second hydrocracking conditions is at least 11°C (20°F) less than the temperature of the first hydrocracking conditions, and wherein the temperature of the first hydrocracking conditions at start-of-run is less than 377°C (710°F).