Process to hydrothermally produce gases from residue streams using a series of reactors
View Patent ↗A process for hydrogen production, the process comprising the steps of mixing hot water and hot oil to produce a mixed stream; increasing a temperature of the mixed stream to produce a reactor feed; upgrading the reactor feed in the non-catalytic reactor to produce a non-catalytic effluent, wherein a temperature in non-catalytic reactor is between 375° C. and 500° C., wherein the non-catalytic reactor is in the absence of catalyst; upgrading the catalytic feed in the catalytic reactor to produce a reactor effluent, wherein a temperature in catalytic reactor is between 550° C. and 700° C., wherein the catalyst is selected from the group consisting of transition metal oxides, lanthanide oxides, and combinations of the same, separating the reactor effluent in the high pressure separator to produce a gases stream; and separating the gases stream in the gases separator to produce a gas product and a light hydrocarbon stream.
1 . A system for hydrogen production, the system comprising:
a mixer configured to mix a hot water and a hot oil to produce a mixed stream;
a combined heater fluidly connected to the mixer, the combined heater configured to increase a temperature of the mixed stream to produce a reactor feed, wherein the temperature of the reactor feed is between 374° C. and 500° C. and the pressure is between 22 MPa and 30 MPa;
a non-catalytic reactor fluidly connected to the combined heater, the non-catalytic reactor configured to upgrade the reactor feed to produce a non-catalytic effluent, wherein a temperature in non-catalytic reactor is between 375° C. and 500° C. and a pressure is between 22 MPa and 30 MPa, wherein the non-catalytic reactor is in the absence of catalyst, wherein hydrocarbons undergo cracking in the non-catalytic reactor;
a catalytic reactor fluidly connected to the non-catalytic reactor, the catalytic reactor configured to upgrade a catalytic feed to produce a reactor effluent, wherein the catalytic feed comprises the non-catalytic effluent mixed with a catalyst, wherein a temperature in the catalytic reactor is between 550° C. and 700° C. and a pressure is between 22 MPa and 30 MPa; wherein the catalyst is selected from the group consisting of transition metal oxides, lanthanide oxides, and combinations of the same, wherein the size of the catalyst is between 1,000 nm and 5,000 nm;
a high pressure separator fluidly connected to the catalytic reactor, the high pressure separator configured to separate the reactor effluent to produce a gases stream and a liquid stream;
a gases separator fluidly connected to the high pressure separator, the gases separator configured to separate the gases stream to produce a gas produce and a light hydrocarbon stream, where the gases stream comprises gases selected from light hydrocarbon gases, hydrogen, carbon monoxide, carbon dioxide, and combinations of the same;
a liquid separator fluidly connected to the high pressure separator, the liquid separator configured to separate the liquid stream to produce a water stream and an upgraded hydrocarbon stream, wherein the water stream comprises water and spent catalyst, wherein the upgraded hydrocarbon stream comprises upgraded hydrocarbons; and
a regeneration unit fluidly connected to the liquid separator, the regeneration unit configured to regenerate spent catalyst in the water stream, wherein regeneration occurs at a temperature between 750° C. and 850° C. and a pressure between 3 bar and 6 bar such that contaminants are removed from the spent catalyst.
2 . The system of claim 1 , further comprising:
a water pump configured to increase a pressure of a water stream to produce a pressurized water, where a pressure of the pressurized water is between 22 MPa and 30 MPa; and
a water heater fluidly connected to the water pump, the water heater configured to increase a temperature of the pressurized water in the water heater to produce the hot water, wherein a temperature of the hot water is between 350° C. and 500° C.
3 . The system of claim 1 , further comprising:
an oil pump configured to increase a pressure of an oil feed to produce a pressurized oil, where a pressure of the pressurized oil is between 22 MPa and 30 MPa; and
an oil heater fluidly connected to the oil pump, the oil heater configured to increase a temperature of the pressurized oil to produce the hot oil, where the temperature of the hot oil is between 100° C. and 380° C.
4 . The system of claim 1 , where the transition metals of the transition metal oxides and lanthanides of the lanthanide metal oxides of the catalyst are selected from the group consisting of nickel, vanadium, cerium, lanthanum, zinc, copper, cobalt, titanium, chromium, and combinations of the same.
5 . The system of claim 1 , wherein the mixer is selected from the group consisting of a standard inline mixer, a static mixer, and combinations of the same.
6 . The system of claim 1 , wherein the non-catalytic reactor is a tubular reactor.
7 . The system of claim 1 , wherein the catalytic reactor is a tubular reactor.