Methanation reactor and method
The present relates to a chemical reactor comprising a catalyst bed enclosed in a reactor vessel and at least one cooling tube placed in the reactor vessel and passing through the catalyst bed, characterized in that the cooling tubes are disposed within the reactor so as to generate thermal gradients of at least 20° C./cm thereby generating hot spots throughout the reactor upon carrying out a reaction. The invention further relates to a methanation process.
1 . A method of production of methane from hydrogen and carbon dioxide comprising the steps of:
a) providing a chemical reactor comprising a reaction chamber which comprises a gas loading zone and a catalyzed reaction zone comprising a catalyst bed;
b) loading a reaction gas mixture of hydrogen and carbon dioxide in the gas loading zone of the reaction chamber, such that the gas pressure in the reaction chamber is between 1 and 20 bar;
c) heating the catalyst bed at a temperature between about 220 and about 260° C. such that the Sabatier reaction and a gas flow through the catalyst bed starts;
d) creating temperature gradients of at least 20° C./cm within the catalyst bed by cooling the catalyst bed with a cooling system directly integrated in said catalyst bed; and
e) collecting the resulting gas mixture flowing through the catalyst bed.
2 . The method according to claim 1 , wherein the chemical reactor comprises a reactor vessel enclosing the catalyst bed and the cooling system comprises cooling tubes placed in the reactor vessel and passing through the catalyst bed, wherein the cooling tubes are disposed within the catalyst bed so as to create the temperature gradients of at least 20° C./cm within the catalyst bed thereby generating hot spots throughout the catalyst bed upon carrying out the Sabatier reaction.
3 . The method according to claim 2 , wherein the catalyst bed comprises at least one of nickel, cobalt and ruthenium based catalysts.
4 . The method according to claim 3 , wherein the catalysts comprises 20% wt. Ni/Al 2 O 3 or 3% wt. Ru/Al 2 O 3 .
5 . The method according to claim 2 , wherein the minimal distance between the tubes is not less than 1.5 times the tube diameter.
6 . The method according to claim 2 , wherein the minimal distance between the tubes is not less than 2 times the tube diameter.
7 . The method according to claim 2 , wherein the temperature of the cooling medium is different in the different tubes.
8 . The method according to claim 2 , wherein the tubes are fed with a cooling medium.
9 . The method according to claim 2 , wherein the temperature gradients are at least 100° C./cm.
10 . The method according to claim 2 , wherein the temperature gradients are controlled by controlling either the space velocity of the inlet reactant gases and/or the flow rate of the cooling medium.
11 . The method according to claim 2 , wherein the chemical reactor further comprises a thermal management system adapted to remove the heat from the reaction zone and to control the temperature of the chemical reactor.
12 . The method according to claim 1 , wherein the chemical reactor further comprises a gas flow system; a heating element in the vicinity of the reaction chamber; a temperature sensing system and a temperature management system, the cooling system comprises a plurality of coolant circulation lines within the catalyst bed, the gas flow system comprises a reaction gas feeding system configured to load reaction gases into the loading zone of the reaction chamber and a reaction gas exhaust system to exhaust reacted gases through the catalyst bed which is thermo-regulated by the heating element and the cooling system under the control of the temperature management system.
13 . The method according to claim 12 , wherein the cooling system comprises a cooling inlet for the coolant flow, a coolant circulation line, a coolant outlet and a coolant flow controlling means.
14 . The method according to claim 12 , wherein the cooling system further comprises a coolant exhaust system to allow controlling the cooling line pressure and maintaining its pressure lower than 5 bar or lower than 1.5 bar.
15 . The method according to claim 12 , wherein the gas flow system allows loading the reaction gases within the gas loading zone of the reaction chamber through a reaction gas feeding system comprising pressure regulating elements and exhausting the reacted gases from the catalyzed reaction zone of the reaction chamber through a reaction gas exhaust system comprising pressure regulating elements.
16 . The method according to claim 12 , wherein the chemical reactor further comprises a condenser system on or after the reaction gas exhaust system to eliminate water by condensation from the reacted gases.