Ammonia production method
High purity hydrogen is produced by a steam reforming hydrogen production unit with at least one of a bayonet reactor for reforming steam and a hydrocarbon, a recuperative burner, and a regenerative burner such that the steam reforming unit produces little or no steam in excess of the steam reforming process requirements. High purity hydrogen is separated from the syngas exiting the reformer via a pressure swing adsorption unit and combined with high purity nitrogen from an air separation unit as feedstock to a Haber process ammonia synthesis unit. Compressors for the ammonia synthesis unit are driven by higher efficiency drivers than are possible using the low temperature steam conventionally exported from a steam reforming unit. Compression power requirements are reduced.
1. A method of producing ammonia within a combination of a hydrogen production unit and a Haber process unit, the method comprising:
reforming reactants of steam and a hydrocarbon feedstock in a bayonet reforming reactor tube in the hydrogen production unit to produce a reformate syngas at a first temperature;
cooling the reformate within the bayonet reforming reactor tube to a second temperature lower than the first temperature;
separating the reformate syngas in a pressure swing adsorption unit to produce a high purity hydrogen stream containing at least 90% hydrogen by volume and a tail gas stream;
separating air in an air separation unit to produce a high purity nitrogen stream containing at least 90% nitrogen by volume;
combining the high purity hydrogen stream and the high purity nitrogen stream into a mixture; and
compressing and processing the mixture in a Haber process unit comprising at least one compressor,
wherein at least 90% of the steam is consumed in the hydrogen production unit to produce the high purity hydrogen stream.
2. The method of claim 1 , wherein the steam is generated by cooling the reformate syngas against boiler feed water in one or more heat exchangers.
3. The method of claim 2 , wherein the one or more heat exchangers comprise:
a first feed water heat exchanger configured to transfer heat from the reformate syngas to heat the boiler feed water; and
a second feed water heat exchanger configured to transfer heat from the reformate syngas to vaporize the heated boiler feed water;
wherein the reformate syngas passes through the second feed water heat exchanger before passing through the first feed water heat exchanger.
4. The method of claim 1 , wherein the at least one compressor is driven by a driver comprising at least one of a gas turbine, a steam turbine utilizing inlet steam at a temperature greater than 550° C., a combined cycle turbine set, or an electric motor.
5. The method of claim 1 , wherein the bayonet reforming reactor tube is heated at least in part by combustion of the tail gas stream.
6. The method of claim 1 , wherein processing the mixture in the Haber process unit yields liquid ammonia and a remainder gaseous mixture, and wherein at least a portion of the remainder gaseous mixture is recycled within the Haber process unit.
7. The method of claim 6 , wherein the bayonet reforming reactor tube is heated at least in part by combustion of a portion of the remainder gaseous mixture.
8. A method of producing ammonia within a combination of a hydrogen production unit and a Haber process unit, the method comprising:
reforming reactants of steam and a hydrocarbon feedstock to produce a reformate syngas in steam reforming reactor at least partially disposed within a furnace of the hydrogen production unit;
separating the reformate syngas in a pressure swing adsorption unit to produce a high purity hydrogen stream containing at least 90% hydrogen by volume and a tail gas stream;
separating air in an air separation unit to produce a high purity nitrogen stream containing at least 90% nitrogen by volume;
combining the high purity hydrogen stream and the high purity nitrogen stream into a mixture; and
compressing and processing the mixture in a Haber process unit containing at least one compressor,
wherein the furnace of the hydrogen production unit is heated by a burner and a heat exchanger, and
wherein combustion air for the burner is preheated to at least 500° C. in the heat exchanger against combustion products of the furnace.
9. The method of claim 8 , wherein at least 90% of the steam is consumed in the hydrogen production unit to produce the high purity hydrogen stream.
10. The method of claim 9 , wherein the steam is generated by cooling the reformate syngas against boiler feed water in one or more heat exchangers.
11. The method of claim 10 , wherein the one or more heat exchangers comprise:
a first feed water heat exchanger configured to transfer heat from the reformate syngas to heat the boiler feed water; and
a second feed water heat exchanger configured to transfer heat from the reformate syngas to vaporize the heated boiler feed water;
wherein the reformate syngas passes through the second feed water heat exchanger before passing through the first feed water heat exchanger.
12. The method of claim 8 , wherein the at least one compressor is driven by a driver comprising at least one of a gas turbine, a steam turbine utilizing inlet steam at a temperature greater than 550° C., a combined cycle turbine set, or an electric motor.
13. The method of claim 8 , wherein the furnace is heated at least in part by combustion of the tail gas stream.
14. The method of claim 8 , wherein processing the mixture in the Haber process unit yields liquid ammonia and a remainder gaseous mixture, and wherein at least a portion of the remainder gaseous mixture is recycled within the Haber process unit.
15. The method of claim 14 , wherein the furnace is heated at least in part by combustion of a portion of the remainder gaseous mixture.
16. The method of claim 8 , wherein the steam reforming reactor comprises a single pass reforming reactor tube.
17. The method of claim 8 , wherein the steam reforming reactor comprises a bayonet reforming reactor tube.