A process for the production of light olefins and aromatics from a hydrocarbon feedstock, comprising the following steps of: (a) feeding a hydrocarbon feedstock into a reaction area for ringopening, wherein the process conditions in said reaction area for ring opening are a temperature from 300[deg.] C. to 500[deg.] C. and a pressure from 2 to 10 MPa together with from 100 to 300 kg of hydrogen per 1,000 kg of feedstock over an aromatic hydrogenation catalyst, said aromatic hydrogenation catalyst comprises from 0.0001 to 5 weight % of one or more metals selected from the group consisting of Ni, W, and Mo, and passing the resulting stream to a ring cleavage unit at a temperature from 200[deg.] C. to 600[deg.] C. and a pressure from 1 to 12 MPa together with from 50 to 200 kg of hydrogen per 1,000 kg of said resulting stream over a ring cleavage catalyst, said ring cleavage catalyst comprises from 0.0001 to 5 weight % of one or more metals selected from the group consisting of Pd, Ru, Is, Os, Cu, Co, Ni, Pt, Fe, Zn, Ga, In, Mo, W, and V on a support selected from the group of synthetic zeolites having the characteristics of ZSM-5, ZSM-11, ZSM-12, ZSM-23, Beta and MCM-22; (b) separating reaction products, which are generated from said reaction area, into an overhead stream and a side stream; (c) feeding the side stream from (b) to a gasoline hydrocracker unit operating at a temperature range of 300-580 °C, a Weight Hourly Space Velocity (WHSV) of 0.1-10 h-1 and a pressure range of 0,3-5 MPa, wherein said gasoline hydrocracker unit is operated at a temperature higher than said ring opening reaction area, and wherein said gasoline hydrocracker unit is operated at a pressure lower than said ring opening reaction area, (d) separating reaction products of said GHC of step (c) into an overhead gas stream, comprising C2-C4 paraffins, hydrogen and methane and a stream comprising aromatic hydrocarbon compounds and non-aromatic hydrocarbon compounds, (e) feeding the overhead gas stream from the gasoline hydrocracker unit into a steam cracker unit. (a) feeding a hydrocarbon feedstock into a reaction area for ringopening, wherein the process conditions in said reaction area for ring opening are a temperature from 300[deg.] C. to 500[deg.] C. and a pressure from 2 to 10 MPa together with from 100 to 300 kg of hydrogen per 1,000 kg of feedstock over an aromatic hydrogenation catalyst, said aromatic hydrogenation catalyst comprises from 0.0001 to 5 weight % of one or more metals selected from the group consisting of Ni, W, and Mo, and passing the resulting stream to a ring cleavage unit at a temperature from 200[deg.] C. to 600[deg.] C. and a pressure from 1 to 12 MPa together with from 50 to 200 kg of hydrogen per 1,000 kg of said resulting stream over a ring cleavage catalyst, said ring cleavage catalyst comprises from 0.0001 to 5 weight % of one or more metals selected from the group consisting of Pd, Ru, Is, Os, Cu, Co, Ni, Pt, Fe, Zn, Ga, In, Mo, W, and V on a support selected from the group of synthetic zeolites having the characteristics of ZSM-5, ZSM-11, ZSM-12, ZSM-23, Beta and MCM-22; (b) separating reaction products, which are generated from said reaction area, into an overhead stream and a side stream; (c) feeding the side stream from (b) to a gasoline hydrocracker unit operating at a temperature range of 300-580 °C, a Weight Hourly Space Velocity (WHSV) of 0.1-10 h-1 and a pressure range of 0,3-5 MPa, wherein said gasoline hydrocracker unit is operated at a temperature higher than said ring opening reaction area, and wherein said gasoline hydrocracker unit is operated at a pressure lower than said ring opening reaction area, (d) separating reaction products of said GHC of step (c) into an overhead gas stream, comprising C2-C4 paraffins, hydrogen and methane and a stream comprising aromatic hydrocarbon compounds and non-aromatic hydrocarbon compounds, (e) feeding the overhead gas stream from the gasoline hydrocracker unit into a steam cracker unit.