Process with continuous catalytic regeneration for treating a hydrocarbon feedstock
The invention relates to a process for the catalytic treatment of a hydrocarbon feedstock with continuous catalytic regeneration, in which process said feedstock is successively circulated in a plurality of reaction zones in series (R 1 , R 2 , R 3 , R 4 ), the catalyst circulating as a moving bed successively in the plurality of reaction zones and flowing from the upstream end to the downstream end of each of the reaction zones and being transported by a carrier gas phase g 1 from the downstream end of one reaction zone to the upstream end of the next reaction zone, characterized in that said carrier gas phase g 1 has a density of greater than or equal to 1 kg/m 3 .
1 . A process for the catalytic reforming or dehydrogenation of a hydrocarbon feedstock with continuous catalytic regeneration, in which process said feedstock is successively circulated in a plurality of reaction zones in series (R 1 , R 2 , R 3 , R 4 ), a catalyst circulating in a moving bed successively in the plurality of reaction zones in series (R 1 , R 2 , R 3 , R 4 ) and flowing from an upstream end to a downstream end of each of the reaction zones and being transported by a carrier gas phase g 1 from the downstream end of one reaction zone to the upstream end of the next reaction zone, wherein said carrier gas phase g 1 has a density, measured under operating conditions at a temperature T of between 20° and 550° C., and at an absolute pressure P of between 0.1 and 0.7 MPa, which is greater than 1 kg/m 3 ,
wherein
said carrier gas phase g 1 comprises at least one gas having a molar mass higher than that of hydrogen, which originates from the reforming process itself, as recycling reagent or product or by-product of the reforming,
or
the temperature of said carrier gas phase g 1 is adjusted to a temperature T3 below 200° C. to increase the density thereof,
or
the pressure of said carrier gas phase g 1 is adjusted to a pressure P3 of at least 1 MPa to increase the density thereof.
2 . The process according to claim 1 , wherein the process is for catalytic reforming, treating a feedstock comprising naphtha to produce aromatic hydrocarbons and/or petrols, or for catalytic dehydrogenation, treating a feedstock comprising paraffin to produce olefins.
3 . The process according to claim 1 , wherein said carrier gas phase g 1 has a density at least 30% greater than that of the hydrogen measured at the same temperature T of between 20° and 550° C., and at the same absolute pressure P of between 0.1 and 0.7 MPa.
4 . The process according to claim 1 , wherein said carrier gas phase g 1 comprises nitrogen and/or at least one C1-C6 light hydrocarbon.
5 . The process according to claim 1 , wherein said carrier gas phase g 1 comprises at least 25% by volume of gas having a molar mass greater than that of hydrogen.
6 . The process according to claim 1 , wherein said carrier gas phase g 1 comprises only one gas having a molar mass greater than that of hydrogen.
7 . The process according to claim 1 , wherein the at least one gas having a molar mass higher than that of hydrogen originates from the reforming process itself, as recycling reagent or product or by-product of the reforming.
8 . The process according to claim 1 , wherein the temperature of said carrier gas phase g 1 is adjusted to a temperature T3 below 200° C. and 150° C., to increase the density thereof.
9 . The process according to claim 1 , wherein the pressure of said carrier gas phase g 1 is adjusted to a pressure P3 of at least 1 MPa to increase the density thereof.
10 . The process according to claim 1 , wherein the reaction zones are located, respectively, in reactors (R 1 , R 2 , R 3 , R 4 ) arranged side-by-side, or are superposed on each other, the catalyst flowing continuously in each reactor from its upstream top end to its downstream bottom end, then being transported by said carrier gas phase via a fluid connection from the downstream bottom end of one reactor to the upstream top end of the next reactor of the series of reactors.
11 . The process according to claim 10 , wherein the fluid connection includes one or more pipes connecting at least one outlet of one reactor to at least one inlet of the next reactor, and optionally vessels or pots.
12 . The process according to claim 1 , wherein the catalyst is transported via a regeneration gas phase g 2 from the downstream end of the last reaction section (R 4 ) of the series of reaction sections to a regeneration zone (RG) and from the regeneration zone to the upstream end of the first reaction zone (R 1 ) of the series of reaction sections (R 1 , R 2 , R 3 , R 4 ), with optional purging of the catalyst of any non-inert gas before it is transported to the regeneration zone.
13 . The process according to claim 12 , wherein the regeneration gas phase g 2 and the carrier phase g 1 have the same composition and/or are under the same temperature and/or pressure conditions.
14 . The process according to claim 1 , wherein the temperature of said carrier gas phase g 1 is adjusted to a temperature T3 between 50° C. and 150° C. to increase the density thereof.
15 . The process according to claim 1 , wherein the pressure of said carrier gas phase g 1 is adjusted to a pressure P3 of between 1.5 MPa and 4 MPa to increase the density thereof.
16 . The process according to claim 1 , wherein said carrier gas phase g 1 has a density, measured under operating conditions at a temperature T of between 20° and 550° C., and at an absolute pressure P of between 0.1 and 0.7 MPa, which is greater than or equal to 1.2 kg/m 3 and not more than 5 kg/m 3 .
17 . The process according to claim 1 , wherein said carrier gas phase g 1 has a density at least two times greater than that of the hydrogen measured at the same temperature T of between 20° and 550° C., and at the same absolute pressure P of between 0.1 and 0.7 MPa.
18 . The process according to claim 1 , wherein said carrier gas phase g 1 comprises at least 80% by volume of gas having a molar mass greater than that of hydrogen.
19 . The process according to claim 1 , wherein the temperature of said carrier gas phase g 1 is adjusted to a temperature T3 between 50° C. and 150° C. to increase the density thereof.
20 . The process according to claim 1 , wherein the pressure of said carrier gas phase g 1 is adjusted to a pressure P3 of between 1.5 MPa and 4 MPa to increase the density thereof.