A process for the regeneration of an adsorber comprising the following steps a) to f): a) regenerating the adsorber by contact with a gaseous stream comprising at least one alkane, b) collecting the outflow of the adsorber in a device, wherein the outflow comprises condensate of stream and an organic composition comprising at least one olefin, at least one alkane and at least one compound containing oxygen and/or sulphur, c) replacing the stream in the adsorber completely or at least partially by the content of the device, d) feeding the adsorber with an organic composition comprising at least one olefin, at least one alkane and at least one compound containing oxygen and/or sulfur, wherein the load of the adsorber with organic composition is increased gradually and the organic composition is routed through the device before being fed into the adsorber, e) hydrogenation of a stream comprising at least one alkane and at least one olefin, carried out prior to step a), to obtain a liquid or gaseous stream, and/or f) converting, prior to step a), the liquid stream into gaseous phase, wherein step a) comprises component step a1) and the further following component steps a2) to a5): a1) heating the adsorber by contact with the gaseous stream, wherein the gaseous stream is condensed within the adsorber, a2) heating the adsorber by contact with the gaseous stream up to a temperature in the range of 230 to 270°C without any condensation of the gaseous stream within the adsorber, a3) regeneration of the absorber at a temperature in the range of 230 to 270°C by contact with the gaseous stream, a4) cooling of the adsorber by contact with stream in gaseous state, to a temperature in the range of 80°C to 120°C, and/or a5) cooling of the adsorber by contact with stream in liquid state to a temperature below 80°C, preferably to a temperature in the range of 40 to 60°C, and wherein the adsorber is employed for the adsorption of compounds containing oxygen and/or sulphur out of organic compositions, the adsorbents are selected from the group consisting of molecular sieves with a pore diameter of 4 to 15 Å, synthetic molecular sieves comprising silicium and aluminium as main components, synthetic zeolithes in which other atoms like boron or phosphorus are incorporated in the layer by co-precipitation, aluminium phosphate, silicium dioxide, kieselgur, titanium dioxide, zirconium dioxide and aluminum oxide and wherein the stream comprises not more than 1000 wt ppm olefin and at least 99 wt.-% of at least one alkane. a) regenerating the adsorber by contact with a gaseous stream comprising at least one alkane, b) collecting the outflow of the adsorber in a device, wherein the outflow comprises condensate of stream and an organic composition comprising at least one olefin, at least one alkane and at least one compound containing oxygen and/or sulphur, c) replacing the stream in the adsorber completely or at least partially by the content of the device, d) feeding the adsorber with an organic composition comprising at least one olefin, at least one alkane and at least one compound containing oxygen and/or sulfur, wherein the load of the adsorber with organic composition is increased gradually and the organic composition is routed through the device before being fed into the adsorber, e) hydrogenation of a stream comprising at least one alkane and at least one olefin, carried out prior to step a), to obtain a liquid or gaseous stream, and/or f) converting, prior to step a), the liquid stream into gaseous phase, a1) heating the adsorber by contact with the gaseous stream, wherein the gaseous stream is condensed within the adsorber, a2) heating the adsorber by contact with the gaseous stream up to a temperature in the range of 230 to 270°C without any condensation of the gaseous stream within the adsorber, a3) regeneration of the absorber at a temperature in the range of 230 to 270°C by contact with the gaseous stream, a4) cooling of the adsorber by contact with stream in gaseous state, to a temperature in the range of 80°C to 120°C, and/or a5) cooling of the adsorber by contact with stream in liquid state to a temperature below 80°C, preferably to a temperature in the range of 40 to 60°C, and wherein the adsorber is employed for the adsorption of compounds containing oxygen and/or sulphur out of organic compositions, the adsorbents are selected from the group consisting of molecular sieves with a pore diameter of 4 to 15 Å, synthetic molecular sieves comprising silicium and aluminium as main components, synthetic zeolithes in which other atoms like boron or phosphorus are incorporated in the layer by co-precipitation, aluminium phosphate, silicium dioxide, kieselgur, titanium dioxide, zirconium dioxide and aluminum oxide and wherein the stream comprises not more than 1000 wt ppm olefin and at least 99 wt.-% of at least one alkane.