hhgo is withdrawn from hhgo draw 38 of fractionation column 14 from a final separation tray located directly above the flash zone 24 the hhgo is then pumped down to flash zone 24 to be utilized by the spray nozzles 54 as previously mentioned the coke drum vapors from inlet 26 are contacted with hhgo from spray nozzles 54 to condense the heavier components from the incoming coker vapor stream most of the hhgo is vaporized by contact with incoming vapors and the heaviest components of the coke drum vapors are condensed heavy coker gas oil is withdrawn from fractionator 14 via heavy coker gas oil draw 36 a portion of the heavy coker gas oil is pumped down to lower separation trays via heavy coker gas oil pump down line 40 a portion of the heavy coker gas oil is sent off as product and the remaining portion of heavy coker gas oil is pumped through heat exchangers 12 to preheat the fresh feed from fresh feed line 20 a portion of the heavy coker gas oil exiting the heat exchangers 12 is diverted and introduced onto the hhgo draw tray immediately above the flash zone 24 to be utilized as tray quench to prevent coke deposition in the hhgo draw tray the remaining heavy coker gas oil exiting heat exchanger 12 is introduced to a number of separation trays located above the heavy coker gas oil draw 36 fig1 a provides a further exemplary embodiment of the present invention upon exiting the hhgo draw 38 tray of the fractionation column 14 a portion of the hhgo is sent to hcgo product thus allowing for further reduction of natural recycle at the expense of the hcgo quality while ensuring the reliable operation of the hhgo trays fig1 b.