A process for manufacturing, from dialkyl maleates and hydrogen, 1,4-butanediol, gamma-butyrolactone and tetrahydrofuran, said process comprising the following steps: a) hydrogenating a stream of dialkyl maleate in a first stage of reaction over suitable catalyst to produce dialkyl succinate; b) further hydrogenating the dialkyl succinate in a second stage of reaction, by using a different suitable catalyst, for producing mainly 1,4-butanediol, together with gamma-butyrolactone and tetrahydrofuran as co-products; wherein, the catalyst used in the first stage of reaction is a low content palladium catalyst supported on carbon or on alumina, the catalyst used for hydrogenolysis in the second stage is a copper containing catalyst, such as copper-chromite catalyst or copper-zinc oxide catalyst, the first stage of reaction operates from 80 to 130 °C as inlet temperature and from 160 to 190 °C as outlet temperature, from 30 to 80 bar as pressure and with a liquid hourly space velocity from 0.5 to 2.0; the second stage of reaction operates from 160 to 190 °C as inlet temperature, from 30 to 80 bar as pressure and with a liquid hourly space velocity from 0.1 to 0.3, and the hydrogen/organic feed molar ratio is from 30 to 60, in order to obtain that: (i) in both stages of reaction the conditions, as hydrogen/ organic feed ratio, pressure and temperature, are such to maintain the reactors in mixed liquid/vapor phase, (ii) the outlet temperature from first reaction step matches the inlet temperature of the second stage of the reaction, being all the heat of reaction of the first hydrogenation step used for pre-heating at the proper temperature the reactive mixture entering the second stage, (iii) the heat content of the liquid-gas mixture from the second stage of reaction, is first used to generate low pressure steam and then to preheat the mixed feed to the inlet temperature of the first reaction stage, and (iv) no external heat source is needed in the reaction system. a) hydrogenating a stream of dialkyl maleate in a first stage of reaction over suitable catalyst to produce dialkyl succinate; b) further hydrogenating the dialkyl succinate in a second stage of reaction, by using a different suitable catalyst, for producing mainly 1,4-butanediol, together with gamma-butyrolactone and tetrahydrofuran as co-products; the catalyst used in the first stage of reaction is a low content palladium catalyst supported on carbon or on alumina, the catalyst used for hydrogenolysis in the second stage is a copper containing catalyst, such as copper-chromite catalyst or copper-zinc oxide catalyst, the first stage of reaction operates from 80 to 130 °C as inlet temperature and from 160 to 190 °C as outlet temperature, from 30 to 80 bar as pressure and with a liquid hourly space velocity from 0.5 to 2.0; the second stage of reaction operates from 160 to 190 °C as inlet temperature, from 30 to 80 bar as pressure and with a liquid hourly space velocity from 0.1 to 0.3, and the hydrogen/organic feed molar ratio is from 30 to 60, in order to obtain that: (i) in both stages of reaction the conditions, as hydrogen/ organic feed ratio, pressure and temperature, are such to maintain the reactors in mixed liquid/vapor phase, (ii) the outlet temperature from first reaction step matches the inlet temperature of the second stage of the reaction, being all the heat of reaction of the first hydrogenation step used for pre-heating at the proper temperature the reactive mixture entering the second stage, (iii) the heat content of the liquid-gas mixture from the second stage of reaction, is first used to generate low pressure steam and then to preheat the mixed feed to the inlet temperature of the first reaction stage, and (iv) no external heat source is needed in the reaction system. (i) in both stages of reaction the conditions, as hydrogen/ organic feed ratio, pressure and temperature, are such to maintain the reactors in mixed liquid/vapor phase, (ii) the outlet temperature from first reaction step matches the inlet temperature of the second stage of the reaction, being all the heat of reaction of the first hydrogenation step used for pre-heating at the proper temperature the reactive mixture entering the second stage, (iii) the heat content of the liquid-gas mixture from the second stage of reaction, is first used to generate low pressure steam and then to preheat the mixed feed to the inlet temperature of the first reaction stage, and (iv) no external heat source is needed in the reaction system.