Methods and systems for the conversion of carbon dioxide to chemicals and/or fuels utilizing steam electrolysis
A method includes heating a steam feed stream received from a reactor unit in a first heat exchanger using an anode effluent from an anode of an electrolyzer as a heat transfer medium to generate a first heated steam effluent, heating the first heated steam effluent in a second heat exchanger using a cathode effluent from a cathode of the electrolyzer as a heat transfer medium to generate a second heated steam effluent, combusting, in a combustion unit, a first tail gas stream to transfer heat to the second heated steam effluent to generate a third heated steam effluent, and passing the third heated steam effluent to the cathode of the electrolyzer.
1. A method, comprising:
heating a steam feed stream having a temperature of from about 250° C. to about 350° C. received from a reactor unit in a first heat exchanger using an anode effluent from an anode of an electrolyzer comprising an anode, a cathode, and an electrolyte inserted between the anode and the cathode as a heat transfer medium to generate a first heated steam effluent having a temperature of about 350° C. to about 450° C. and a cooled anode effluent;
heating the first heated steam effluent in a second heat exchanger using a cathode effluent from the cathode of the electrolyzer as a heat transfer medium to generate a second heated steam effluent having a temperature of about 550° C. to about 650° C. and a cooled cathode effluent;
combusting, in a combustion unit, a first tail gas stream to transfer heat to the second heated steam effluent to generate a third heated steam effluent having a temperature of about 700° C. to about 950° C.; and
passing the third heated steam effluent to the cathode of the electrolyzer.
2. The method according to claim 1 , further comprising:
heating a water feed stream in a third heat exchanger using a reactor synthesis effluent from the reactor unit as a heat transfer medium to generate a heated water effluent having a temperature of about 50° C. to about 150° C.;
introducing the heated water effluent, a heated carbon dioxide stream, the cooled cathode effluent and a tail gas stream to the reactor unit; and
performing an exothermic reaction of the heated carbon dioxide stream, the cooled cathode effluent and the tail gas stream in the reactor unit, thereby transferring heat from the exothermic reaction to the heated water effluent to generate the steam feed stream.
3. The method according to claim 2 , wherein performing an exothermic reaction of the heated carbon dioxide stream, the cooled cathode effluent and the tail gas stream in the reactor unit comprises direct hydrogenation of carbon dioxide to one of methanol or dimethyl ether.
4. The method according to claim 1 , further comprising:
heating a water feed stream in a third heat exchanger using a reactor synthesis effluent from the reactor unit as a heat transfer medium to generate a heated water effluent having a temperature of about 50° C. to about 150° C.;
introducing the heated water effluent, the cooled cathode effluent, syngas including carbon monoxide and hydrogen received from a reverse water gas shift reaction unit and a tail gas stream to the reactor unit; and
performing an exothermic reaction of the cooled cathode effluent, the syngas and the tail gas stream in the reactor unit, thereby transferring heat from the exothermic reaction to the heated water effluent to generate the steam feed stream.
5. The method according to claim 1 , further comprising:
heating a carbon dioxide stream in a third heat exchanger using the cooled anode effluent from the first heat exchanger as a heat transfer medium to generate a heated carbon dioxide effluent having a temperature of about 250° C. to about 350° C.;
heating an anode purge stream in a fourth heat exchanger using the cooled cathode effluent as a heat transfer medium to generate a first heated anode purge stream having a temperature of about 350° C. to about 450° C. and another cooled cathode effluent;
generating syngas by a reverse water gas shift reaction of the heated carbon dioxide effluent, the other cooled cathode effluent and a tail gas stream; and
introducing the syngas to the reactor unit.
6. The method according to claim 4 , wherein the exothermic reaction in the reactor unit comprises converting the syngas to a chemical product or a fuel.
7. The method according to claim 6 , wherein the chemical product is one or more of methanol and dimethyl ether and the fuel is one or more of gasoline, diesel, and jet fuel.
8. The method according to claim 4 , wherein the exothermic reaction in the reactor unit comprises converting the syngas to a Fischer-Tropsch product.
9. The method according to claim 4 , wherein the exothermic reaction in the reactor unit comprises converting the syngas, the cooled cathode effluent and the tail gas stream to a reactor synthesis effluent including tail gas, and the method further comprises:
splitting the synthesis effluent into a first reactor synthesis effluent and a second reactor synthesis effluent;
heating the water feed stream in the third heat exchanger using the first reactor synthesis effluent as a heat transfer medium to generate the heated water effluent and a cooled first reactor synthesis effluent;
cooling the second reactor synthesis effluent in a fourth heat exchanger to generate a cooled second reactor synthesis effluent;
combining the cooled first reactor synthesis effluent and the cooled second reactor synthesis effluent to form a third cooled reactor synthesis effluent;
separating the tail gas from the third cooled reactor synthesis effluent to generate a third tail gas stream; and
passing the third tail gas stream to the combustion unit to generate combustion heat and hot flue gas for further potential heat integration.
10. The method according to claim 5 , further comprising:
heating the first heated anode purge stream in a fifth heat exchanger using the anode effluent from the anode of the electrolyzer as a heat transfer medium to generate a second heated anode purge stream having a temperature of from about 550° C. to about 650° C.; and
heating the second heated anode purge stream in a sixth heat exchanger using a combustion effluent from the combustion unit as a heat transfer medium to generate a third heated anode purge stream having a temperature of about 700° C. to about 950° C. for sending to the anode of the electrolyzer.
11. The method according to claim 1 , wherein the electrolyzer is a solid oxide steam electrolyzer.
12. A method, comprising:
heating a water feed stream in a first heat exchanger using a reactor synthesis effluent including tail gas from a reactor unit as a heat transfer medium to generate a heated water effluent having a temperature of about 50° C. to about 150° C.;
performing an exothermic reaction in the reactor unit thereby transferring heat from the exothermic reaction to the heated water effluent to generate a steam feed stream having a temperature of about 250° C. to about 350° C.;
heating the steam feed stream in a second heat exchanger using an anode effluent from an anode of an electrolyzer comprising an anode, a cathode, and an electrolyte inserted between the anode and the cathode as a heat transfer medium to generate a first heated steam effluent having a temperature of about 350° C. to about 450° C. and a cooled anode effluent;
heating the first heated steam effluent in a third heat exchanger using a cathode effluent from the cathode of the electrolyzer as a heat transfer medium to generate a second heated steam effluent having a temperature of about 550° C. to about 650° C. and a cooled cathode effluent;
combusting, in a combustion unit, a first tail gas stream to transfer heat to the second heated steam effluent to generate a third heated steam effluent having a temperature of about 700° C. to about 950° C.; and
passing the third heated steam effluent to the cathode of the electrolyzer.
13. The method according to claim 12 , further comprising:
heating a carbon dioxide stream in a fourth heat exchanger using the cooled anode effluent from the second heat exchanger as a heat transfer medium to generate a heated carbon dioxide effluent having a temperature of about 250° C. to about 350° C.;
heating an anode purge stream in a fifth heat exchanger using the cooled cathode effluent from the third heat exchanger as a heat transfer medium to generate a first heated anode purge stream having a temperature of about 350° C. to about 450° C. and another cooled cathode effluent;
generating syngas by a reverse water gas shift reaction of the heated carbon dioxide effluent, the other cooled cathode effluent and a tail stream; and
introducing the syngas to the reactor unit.
14. The method according to claim 13 , further comprising:
heating the first heated anode purge stream in a sixth heat exchanger using the anode effluent from the anode of the electrolyzer as a heat transfer medium to generate a second heated anode purge stream having a temperature of from about 550° C. to about 650° C.; and
heating the second heated anode purge stream in a seventh heat exchanger using a combustion effluent from the combustion unit as a heat transfer medium to generate a third heated anode purge stream having a temperature of about 700° C. to about 950° C. for sending to the anode of the electrolyzer.
15. The method according to claim 13 , wherein the exothermic reaction in the reactor unit comprises converting the syngas to a chemical product or a fuel.
16. The method according to claim 13 , wherein the exothermic reaction in the reactor unit comprises converting the syngas to a Fischer-Tropsch product.
17. The method according to claim 12 , wherein performing an exothermic reaction in the reactor unit comprises direct hydrogenation of a heated carbon dioxide stream, the cooled cathode effluent and a tail gas stream in the reactor unit to generate one of methanol or dimethyl ether.
18. The method according to claim 12 , wherein the electrolyzer is a solid oxide steam electrolyzer.