Process for the isomerizing dehydration of a feedstock comprising from 40% to 100% by weight of primary alcohol substituted in position 2 with an alkyl group, comprising at least the following steps: a) placing said feedstock under pressure, followed by mixing a fraction of said compressed feedstock with the alcohol-rich organic effluent obtained from step h) and with a fraction of the aqueous effluent obtained from step f), followed by preheating said mixture, so as to produce a partially vaporized feedstock, the residual fraction of compressed feedstock being sent into step h); b) vaporization and final superheating of said partially vaporized feedstock to a temperature of between 250 and 375°C so as to produce a vaporized feedstock; c) dehydration of said vaporized feedstock in at least one dehydration reactor operating in the gas phase at a weighted mean temperature of between 250 and 375°C, at a pressure of between 0.2 MPa and 1 MPa and at a WHSV of between 1 and 18 h -1, in the presence of a catalyst comprising a zeolite containing at least one series of channels whose aperture is defined by a ring containing 8 oxygen atoms, said catalyst being coked in-situ or ex-situ beforehand, so as to produce a dehydration effluent; d) cooling of said dehydration effluent obtained from step c) to a temperature of between 30 and 50°C, so as to produce a cooled effluent; e) separation by settling of said cooled effluent as an aqueous phase and an organic phase; f) separation by distillation of said aqueous phase obtained from step e) so as to produce a light hydrocarbon effluent comprising at least 50% by weight of hydrocarbons comprising not more than 4 carbon atoms and an aqueous effluent, a fraction of said aqueous effluent being purged, the other part being recycled into step a); g) separation by distillation of said organic phase obtained from step e) so as to produce an olefinic effluent comprising at least 50% by weight of olefins corresponding to primary alcohol(s) substituted in position 2 with an alkyl group, fed into said feedstock, and a heavy hydrocarbon effluent; h) mixing of the heavy hydrocarbon effluent obtained from step g) with the residual fraction of compressed feedstock obtained from step a), the flow rate of said residual fraction being adjusted so that the mass ratio of the flows of residual fraction to unconverted alcohol in a heavy hydrocarbon effluent is between 2:1 and 10:1, followed by separation by distillation of said mixture so as to produce a C5-C6 hydrocarbon effluent, an alcohol-rich organic effluent and a C6+ hydrocarbon effluent, and recycling of said alcohol-rich organic effluent into step a). a) placing said feedstock under pressure, followed by mixing a fraction of said compressed feedstock with the alcohol-rich organic effluent obtained from step h) and with a fraction of the aqueous effluent obtained from step f), followed by preheating said mixture, so as to produce a partially vaporized feedstock, the residual fraction of compressed feedstock being sent into step h); b) vaporization and final superheating of said partially vaporized feedstock to a temperature of between 250 and 375°C so as to produce a vaporized feedstock; c) dehydration of said vaporized feedstock in at least one dehydration reactor operating in the gas phase at a weighted mean temperature of between 250 and 375°C, at a pressure of between 0.2 MPa and 1 MPa and at a WHSV of between 1 and 18 h -1, in the presence of a catalyst comprising a zeolite containing at least one series of channels whose aperture is defined by a ring containing 8 oxygen atoms, said catalyst being coked in-situ or ex-situ beforehand, so as to produce a dehydration effluent; d) cooling of said dehydration effluent obtained from step c) to a temperature of between 30 and 50°C, so as to produce a cooled effluent; e) separation by settling of said cooled effluent as an aqueous phase and an organic phase; f) separation by distillation of said aqueous phase obtained from step e) so as to produce a light hydrocarbon effluent comprising at least 50% by weight of hydrocarbons comprising not more than 4 carbon atoms and an aqueous effluent, a fraction of said aqueous effluent being purged, the other part being recycled into step a); g) separation by distillation of said organic phase obtained from step e) so as to produce an olefinic effluent comprising at least 50% by weight of olefins corresponding to primary alcohol(s) substituted in position 2 with an alkyl group, fed into said feedstock, and a heavy hydrocarbon effluent; h) mixing of the heavy hydrocarbon effluent obtained from step g) with the residual fraction of compressed feedstock obtained from step a), the flow rate of said residual fraction being adjusted so that the mass ratio of the flows of residual fraction to unconverted alcohol in a heavy hydrocarbon effluent is between 2:1 and 10:1, followed by separation by distillation of said mixture so as to produce a C5-C6 hydrocarbon effluent, an alcohol-rich organic effluent and a C6+ hydrocarbon effluent, and recycling of said alcohol-rich organic effluent into step a).