between 650 u00b0 900 u00b0 c preferably 750 u00b0 850 u00b0 c the preheated oxygen source is thereafter admixed with the reformed gas exiting the reformer at a temperature of 950 u00b0 c if necessary conditioning unit 20 can be used to heat the reformed gas from the reformer however under normal operating conditions no additional heating is required as the preheated oxygen source is admixed with the reducing gas partial combustion of the oxygen source takes place the partial combustion raises the temperature of the partially oxidized reducing feed gas stream to a temperature of at least 1100 u00b0 c this temperature increase is controlled by controlling the amount of the oxygen source material preheated and fed to the reducing gas stream in addition to the rise in temperature the partially oxidized reducing feed gas stream has a rise in the degree of oxidation over that of the reformed gas produced in reformer 18 such that the degree of oxidation of the partially oxidized reducing feed gas stream is between 0 10 to 0 17 the partially oxidized reducing feed gas stream as described above is thereafter fed to the reforming reducing zone 34 of the reactor and contacts the dri in the presence of natural gas within the reforming reducing zone in accordance with the present invention natural gas is injected preferably directly into the reforming reducing zone 34 via line 36 for contacting the partially oxidized reducing feed gas stream within the reforming reducing zone 34 wherein the dri in the zone acts as a catalyst for reacting the oxides within the partially oxidized reducing feed gas with the natural gas so as.