An integrating process for conversion of crude oil to light olefins, aromatics, syngas and valuable chemicals, the process comprising: (i) charging the crude oil to a desalter unit to obtain a desalted crude oil; (ii) routing the desalted crude oil to a pre-fractionator column to separate the desalted crude oil in to a lighter hydrocarbon material boiling below 200°C, a hydrocarbon boiling in the range of 200-370°C and a heavier hydrocarbon material boiling above 370°C; (iii) routing the lighter hydrocarbon material to a naphtha cracker unit to obtain a high aromatic gasoline stream; (iv) routing the heavier hydrocarbon material boiling above 370°C from the pre-fractionator column to a delayed coker unit, wherein the hydrocarbon material boiling above 370°C undergoes thermal cracking reaction to obtain a gaseous products containing LPG, lighter product materials boiling in the range of naphtha, coker gasoil stream and solid petroleum coke; (v) routing the hydrocarbons boiling in the range of 200-370°C from the pre-fractionator column and the coker gasoil stream produced in the delayed coker unit to a high severity catalytic cracker unit wherein the hydrocarbons boiling in the range of 200-370°C and the coker gasoil stream undergo catalytic cracking reaction to generate a clarified oil stream, gaseous products containing LPG, light cycle oil product and lighter products boiling in the range of naphtha, wherein the clarified oil stream is subjected to the delayed coker unit; (vi) routing the gaseous products containing LPG generated from the delayed coker unit and the gaseous products containing LPG generated from the high severity catalytic cracking unit to an olefin recovery section to obtain light olefins, wherein the light olefins from the olefin recovery section comprising ethylene, propylene, and butylene are separated and C5-materials other than the light olefins from the olefin recovery section are recycled back to the naphtha cracker unit for complete conversion; (vii) routing the high aromatic gasoline stream generated from the naphtha cracker unit and the light cycle oil product from the high severity catalytic cracking unit to an aromatic recovery section for recovery of aromatic products; and (viii) routing the solid petroleum coke produced in the delayed coker unit to a coke gasifier unit where it is converted to syngas, and the syngas is sent to a chemical production section to obtain a valuable chemicals comprising methanol and light olefins; wherein the lighter product materials boiling in the range of naphtha from the delayed coker unit, the lighter products boiling in the range of naphtha from the high severity catalytic cracker unit, and a paraffinic raffinate stream from the aromatic recovery section are sent to naphtha cracker unit for cracking to a valuable lighter products; wherein the high severity gasoil catalytic cracker unit employs a circulating fluidized bed reactor configuration and a catalyst mixture containing 'large pore bottom selective active material' of pore size more than 50 Å, Y/REY/USY/RE-USY zeolites of medium pore size of 7 to 11 Å and shape selective pentasil zeolite components; wherein the thermal cracking reaction is occurred in the delayed coker unit before the catalytic cracking reaction occurred in the catalytic cracker unit. (i) charging the crude oil to a desalter unit to obtain a desalted crude oil; (ii) routing the desalted crude oil to a pre-fractionator column to separate the desalted crude oil in to a lighter hydrocarbon material boiling below 200°C, a hydrocarbon boiling in the range of 200-370°C and a heavier hydrocarbon material boiling above 370°C; (iii) routing the lighter hydrocarbon material to a naphtha cracker unit to obtain a high aromatic gasoline stream; (iv) routing the heavier hydrocarbon material boiling above 370°C from the pre-fractionator column to a delayed coker unit, wherein the hydrocarbon material boiling above 370°C undergoes thermal cracking reaction to obtain a gaseous products containing LPG, lighter product materials boiling in the range of naphtha, coker gasoil stream and solid petroleum coke; (v) routing the hydrocarbons boiling in the range of 200-370°C from the pre-fractionator column and the coker gasoil stream produced in the delayed coker unit to a high severity catalytic cracker unit wherein the hydrocarbons boiling in the range of 200-370°C and the coker gasoil stream undergo catalytic cracking reaction to generate a clarified oil stream, gaseous products containing LPG, light cycle oil product and lighter products boiling in the range of naphtha, wherein the clarified oil stream is subjected to the delayed coker unit; (vi) routing the gaseous products containing LPG generated from the delayed coker unit and the gaseous products containing LPG generated from the high severity catalytic cracking unit to an olefin recovery section to obtain light olefins, wherein the light olefins from the olefin recovery section comprising ethylene, propylene, and butylene are separated and C5-materials other than the light olefins from the olefin recovery section are recycled back to the naphtha cracker unit for complete conversion; (vii) routing the high aromatic gasoline stream generated from the naphtha cracker unit and the light cycle oil product from the high severity catalytic cracking unit to an aromatic recovery section for recovery of aromatic products; and (viii) routing the solid petroleum coke produced in the delayed coker unit to a coke gasifier unit where it is converted to syngas, and the syngas is sent to a chemical production section to obtain a valuable chemicals comprising methanol and light olefins;